CN102470318A - Device for treating exhaust gas and method for eliminating mercury from exhaust gas - Google Patents

Device for treating exhaust gas and method for eliminating mercury from exhaust gas Download PDF

Info

Publication number
CN102470318A
CN102470318A CN2010800344216A CN201080034421A CN102470318A CN 102470318 A CN102470318 A CN 102470318A CN 2010800344216 A CN2010800344216 A CN 2010800344216A CN 201080034421 A CN201080034421 A CN 201080034421A CN 102470318 A CN102470318 A CN 102470318A
Authority
CN
China
Prior art keywords
flue
gas
waste gas
reduction
mercury
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
CN2010800344216A
Other languages
Chinese (zh)
Other versions
CN102470318B (en
Inventor
四条利久磨
坂田展康
串冈清则
村上盛纪
鹈饲展行
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Mitsubishi Power Ltd
Original Assignee
Mitsubishi Heavy Industries Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Mitsubishi Heavy Industries Ltd filed Critical Mitsubishi Heavy Industries Ltd
Publication of CN102470318A publication Critical patent/CN102470318A/en
Application granted granted Critical
Publication of CN102470318B publication Critical patent/CN102470318B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/75—Multi-step processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/50—Sulfur oxides
    • B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/64—Heavy metals or compounds thereof, e.g. mercury
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8621—Removing nitrogen compounds
    • B01D53/8625—Nitrogen oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8665—Removing heavy metals or compounds thereof, e.g. mercury
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/90—Injecting reactants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
    • B01F25/30—Injector mixers
    • B01F25/31—Injector mixers in conduits or tubes through which the main component flows
    • B01F25/313—Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced in the centre of the conduit
    • B01F25/3132—Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced in the centre of the conduit by using two or more injector devices
    • B01F25/31322—Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced in the centre of the conduit by using two or more injector devices used simultaneously
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
    • B01F25/30—Injector mixers
    • B01F25/31—Injector mixers in conduits or tubes through which the main component flows
    • B01F25/313—Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced in the centre of the conduit
    • B01F25/3133—Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced in the centre of the conduit characterised by the specific design of the injector
    • B01F25/31331—Perforated, multi-opening, with a plurality of holes
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/02—Arrangements of devices for treating smoke or fumes of purifiers, e.g. for removing noxious material
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/20—Reductants
    • B01D2251/206—Ammonium compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/20—Reductants
    • B01D2251/206—Ammonium compounds
    • B01D2251/2062—Ammonia
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/40—Alkaline earth metal or magnesium compounds
    • B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/50—Inorganic acids
    • B01D2251/502—Hydrochloric acid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/60—Inorganic bases or salts
    • B01D2251/606—Carbonates
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/60—Inorganic bases or salts
    • B01D2251/608—Sulfates
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/60—Heavy metals or heavy metal compounds
    • B01D2257/602—Mercury or mercury compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/68—Halogens or halogen compounds
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2215/00—Preventing emissions
    • F23J2215/20—Sulfur; Compounds thereof
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2215/00—Preventing emissions
    • F23J2215/60—Heavy metals; Compounds thereof
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2219/00—Treatment devices
    • F23J2219/10—Catalytic reduction devices
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2219/00—Treatment devices
    • F23J2219/40—Sorption with wet devices, e.g. scrubbers

Abstract

The disclosed device for treating exhaust gas (10) eliminates NOx and Hg contained in exhaust gas (12) from a boiler (11), and has a NH4Cl solution supply means (16) that is in the downstream flue (13) of the boiler (11) and that mists a NH4Cl solution (14) by means of a plurality of misting nozzles (15); a reductive denitrification device (18) that has a denitrification catalyst that reduces NOx in the exhaust gas (12) using NH3 and oxidizes Hg in the presence of HCl; and a wet desulfurization device (22) that eliminates the Hg that had been oxidized by the reductive denitrification device (18) using a lime gypsum slurry (21). The NH4Cl supply means (16) supplies the NH4Cl solution (14) from the misting nozzles (15) so as not to accrue on the inner wall of the flue (13) through which the exhaust gas (12) flows.

Description

The mercury of emission-control equipment and waste gas is removed method
Technical field
The present invention relates to the mercury that from the waste gas of discharges such as boiler, contains is carried out the emission-control equipment of oxidation processes and the mercury of waste gas is removed method.
Background technology
In the waste gas that when coal burns waste gas, burning mink cell focus, produces, except coal dust, oxysulfide (SOx), nitrogen oxide (NOx), also contain mercury metal (Hg sometimes 0).In recent years, for making up with the denitrification apparatus of reducing NOx and the wet desulfurizer of alkali absorption liquid as the SOx absorbent, the method and apparatus that this mercury metal is handled has proposed various schemes.
As the method for handling the mercury metal in the waste gas, a kind of preceding trip side spray ammonia (NH of the high temperature denitrification apparatus in flue has been proposed 3) solution reduces denitration; And oxidation promoters such as spraying hydrochloric acid (HCl) solution; After becoming water miscible mercury chloride, utilization is arranged on the back and swims system's (for example with reference to patent documentation 1) that the wet desulfurizer of side is removed mercury making mercury oxidation (chlorination) on the denitrating catalyst.
In addition; As the method for supplying with HCl; There is a kind of hydrogen chloride (HCl) gasifier that utilizes to make hydrochloric acid (HCl) vaporizer and become hydrogen chloride (HCl) gas; And after the mist that is adjusted to the HCl that contains normal concentration, mist is disperseed in flue, the method for this mist of in the waste gas that contains mercury, spraying equably (for example with reference to patent documentation 2).
In addition, as other the method for supply HCl, have in a kind of flue of the preceding trip side to denitrification apparatus and add ammonium chloride (NH with powder shaped 4Cl), utilize the high-temperature atmosphere temperature of waste gas to make NH 4The Cl distillation, and make HCl, ammonia (NH 3) gasification respectively, with HCl gas, the NH after the gasification 3Gas is mixed into the method (for example with reference to patent documentation 3) in the waste gas.
In the method that the mercury metal in the waste gas of above-mentioned that kind is handled, when using hydrochloric acid solution, because hydrochloric acid is danger, so exist transportation, operation etc. to need the problem of labour and cost.In addition, under the situation of having used the HCl gasifier, need steam etc. as thermal source, existence needs the problem of the expense of equipment, running, maintenances etc. such as HCl gasifier.And, using NH 4Under the situation of Cl powder, particle diameter is fine to be disperseed owing to making, so handle (handling) difficulty, has the very difficult problem of control of spray amount.
[patent documentation 1] japanese kokai publication hei 10-230137 communique
[patent documentation 2] TOHKEMY 2007-167743 communique
[patent documentation 3] TOHKEMY 2008-221087 communique
Given this, studying in order to utilize denitrating catalyst to make Hg in recent years 0Oxidation, and at the preceding trip side spray ammonium chloride (NH of denitrification apparatus 4Cl) method of solution.Compare with the method for using hydrochloric acid solution as in the past, because NH 4Cl solution is dangerous few, thus transportation, processing ease, and, need not be used for the equipment such as gasifier of spraying liquid, thereby can reduce cost.
Figure 29 has represented from the skeleton diagram of the exhaust treatment system of the waste gas of boiler discharge.Shown in figure 29, exhaust treatment system 100 has: NH 4 Cl sprayer unit 105, its in flue 104 to containing NOx, Hg from what be supplied to that boiler 101 that coal acts as a fuel discharges 0Waste gas 102 spraying NH 4Cl solution 103; Reduction denitrification apparatus 106, it possesses the denitrating catalyst that NOx is reduced and Hg carried out oxidation; With desulfurizer 107, it removes the HgCl behind oxidized in the waste gas 102.From NH 4Cl NaOH solution tank NaOH 108 is through spray nozzle 109 NH that in the waste gas 102 of being discharged by boiler 101, sprays 4Cl solution 103, NH 4Cl solution 103 generating gasification make NH 3Gas, HCl gas are mixed in the waste gas 102.Then, waste gas 102 is fed into reduction denitrification apparatus 106, utilizes the denitrating catalyst in the reduction denitrification apparatus 106 to carry out the reduction of NOx, and to Hg 0Carry out oxidation.Then, the waste gas of removing behind the NOx 102 carries out heat exchange through air preheater (air heater) 110 and air 111, and after recuperation of heat, is fed into electrostatic (electric dust) precipitator 112, removes the coal dust in the waste gas 102 after the recuperation of heat.Waste gas 102 is fed into desulfurizer 107, starches 113 gas-liquids with the plaster stone that desulfurizer 107 is provided and contacts, and SOx, Hg are removed, and is discharged to the outside as Purge gas 114 from chimney 115 then.
In addition, be utilized in the NOx concentration that the NOx of the preceding trip side setting of the reduction denitrification apparatus 106 in the flue 104 measures in 116 pairs of waste gas 102 of meter and measure, the concentration of 117 couples of Hg of Hg densimeter that is utilized in the back trip side setting of desulfurizer 107 is measured.Measured value based on the NOx concentration that determines, Hg concentration is calculated from NH by operational part 118 4The NH that Cl NaOH solution tank NaOH 108 is supplied with 4The quantity delivered of Cl solution 103, concentration.Based on the NH that calculates 4The quantity delivered of Cl solution 103, concentration are by the NH that supplies with in the controlling organization 119 subtend flues 104 4The quantity delivered of Cl solution 103 is controlled.
In addition, the 120 pairs of oxidation-reduction potentials of oxidation reduction potential determination device that are utilized in the tower bottom setting of desulfurizer 107 are measured, and adjust the quantity delivered of air 121, and the reduction of carrying out mercury oxide prevents, diffusion preventing.
Like this, through in waste gas 102, supplying with NH 4 Cl solution 103 can be removed the NOx in the waste gas 102, and Hg is carried out oxidation.
Here, in exhaust treatment system shown in Figure 29 100, shown in figure 30; Spray nozzle 109 for example is provided with a plurality of along the wall of flue 104, consider cost and maintainability are set, and the radical of preferred spray nozzle is few; If but very few, NH equably then can't spray in flue 104 4Cl solution 103.Therefore, exist by NH 4The NH that Cl solution 103 produces 3, HCl can not be equably supplies with in waste gas 102, causes the NH in the waste gas 102 3Concentration, HCl density unevenness are spared, the problem that denitration performance and mercury oxidation performance reduce.
In addition, work as NH 4 Cl solution 103 before gasification when being attached to the wall of flue 104, the problems such as breakage that have the accumulation of the burn into ash that flue 104 possibly take place, cause because of thermal shock.
Summary of the invention
The present invention proposes in view of the above problems; Its purpose is; Provide a kind of can be with reducing agent, mercury chlorinating agent concentration is constant in flue, supplies with equably, keep emission-control equipment and the mercury of waste gas of the reducing property of removing performance, nitrogen oxide of mercury and remove method.
In order to solve above-mentioned problem, can adopt following formation.
1) the 1st invention of the present invention relates to a kind of nitrogen oxide contained in will the waste gas from boiler, the emission-control equipment that mercury is removed; Have: reduction-oxidation auxiliary agent feed mechanism, in the flue of the reduction-oxidation auxiliary agent that generates oxidizing gas and reducibility gas when it utilizes a plurality of spray nozzles to gasify with the liquid downstream that are sprayed to above-mentioned boiler; Reduction denitration mechanism, its have with above-mentioned reducibility gas reduce above-mentioned nitrogen oxides from exhaust gas and under above-mentioned oxidizing gas coexistence with the denitrating catalyst of mercury oxidation; With wet type desulfurizing mechanism, the mercury after it utilizes the alkali absorption liquid will be in this reduces denitration mechanism oxidized is removed; Above-mentioned spray nozzle is not attached to the mode of the inwall of above-mentioned flue according to above-mentioned reduction-oxidation auxiliary agent, and above-mentioned reduction-oxidation auxiliary agent is supplied with in above-mentioned flue.
2) emission-control equipment of the 2nd invention is based on the 1st invention; Droplets vaporize according to being obtained by gas flow rate, drop initial velocity, liquid-drop diameter, EGT, drop temperature at least is needed apart from l and spray angle α; Satisfy the mode of following formula according to the beeline x till from the inwall of above-mentioned flue to the nozzle bore of above-mentioned spray nozzle, dispose above-mentioned spray nozzle.
x＞l×sinα…(1)
3) emission-control equipment of the 3rd invention is based on the 1st or the 2nd invention, and above-mentioned reduction-oxidation auxiliary agent is an ammonium chloride.
4) emission-control equipment of the 4th invention is based on any one in the 1st to the 3rd invention, and the nozzle bore of above-mentioned spray nozzle is set at the above position of wall 0.5m of the above-mentioned flue of distance.
5) emission-control equipment of the 5th invention is based on any one in the 1st to the 4th invention, and a plurality of spray nozzles are configured to satisfy following formula.
a≤b/5…(2)
Wherein, a is the nozzle distance between borehole of the nozzle bore of spray nozzle, and b is the length of long side in the cross-sectional length of flue.
6) emission-control equipment of the 6th invention is based on any one in the 1st to the 5th invention, and above-mentioned spray nozzle has the nozzle bore of the above-mentioned reduction-oxidation auxiliary agent of a plurality of sprayings.
7) emission-control equipment of the 7th invention is based on the 6th invention, said nozzle hole being spaced apart below the 0.3m each other.
8) emission-control equipment of the 8th invention can change from the spray amount of each above-mentioned spray nozzle based on any one in the 1st to the 7th invention.
9) emission-control equipment of the 9th invention is based on any one in the 1st to the 8th invention, has to be arranged between above-mentioned reduction-oxidation auxiliary agent feed mechanism and the above-mentioned reduction denitration mechanism and in above-mentioned flue, to supply with the ammonia supply unit of ammonia and in above-mentioned flue, supply with the perhaps both sides of any side in the hydrogen chloride gas supply unit of hydrogen chloride gas.
10) the 10th invention mercury that relates to the waste gas that nitrogen oxide contained in the waste gas from boiler, mercury are removed is removed method; Have: reduction-oxidation auxiliary agent supplying step, the reduction-oxidation auxiliary agent that generates oxidizing gas and reducibility gas when utilizing a plurality of spray nozzles to gasify is with in the liquid flue that is sprayed to above-mentioned boiler; Reduction denitration treatment step use denitrating catalyst, utilizes above-mentioned reducibility gas that above-mentioned nitrogen oxides from exhaust gas is reduced, and under above-mentioned oxidizing gas coexists with mercury oxidation; With the wet type desulfurizing step, the mercury after utilizing the alkali absorption liquid will be in this reduces the denitration treatment step oxidized is removed; Above-mentioned spray nozzle is not attached to the mode of the inwall of above-mentioned flue according to above-mentioned reduction-oxidation auxiliary agent, and above-mentioned reduction-oxidation auxiliary agent is supplied with in above-mentioned flue.
11) mercury of the waste gas of the 11st invention is removed method based on the 10th invention; Droplets vaporize according to being obtained by gas flow rate, drop initial velocity, liquid-drop diameter, EGT, drop temperature at least is needed apart from l and spray angle α; Satisfy the mode of following formula according to the beeline x till from the inwall of above-mentioned flue to the nozzle bore of above-mentioned spray nozzle, dispose above-mentioned spray nozzle.
x＞l×sinα…(3)
12) mercury of the waste gas of the 12nd invention is removed method based on the 10th or the 11st invention, and above-mentioned reduction-oxidation auxiliary agent is an ammonium chloride.
13) mercury of waste gas of the 13rd invention is removed method based on any one in the 10th to the 12nd invention, and the nozzle bore of above-mentioned spray nozzle is arranged on the position more than the distance wall 0.5m of above-mentioned flue.
14) mercury of the waste gas of the 14th invention is removed method based on any one in the 10th to the 13rd invention, and a plurality of spray nozzles are configured to satisfy following formula.
a≤b/5…(4)
Wherein, a is the nozzle distance between borehole of the nozzle bore of spray nozzle, and b is the length of long side in the cross-sectional length of flue.
15) mercury of the waste gas of the 15th invention is removed method based on any one in the 10th to the 14th invention; Have in the flow measurement step of measuring the flow velocity of above-mentioned waste gas than the supply position of supplying with above-mentioned reduction-oxidation auxiliary agent by upstream side, adjust spray amount, spray angle, the initial velocity of above-mentioned reduction-oxidation auxiliary agent based on the flow velocity of the above-mentioned waste gas that determines.
16) mercury of waste gas of the 16th invention is removed method based on any one in the 10th to the 15th invention, comprising: the nitrous oxides concentration determination step of the concentration of above-mentioned nitrogen oxides of exhaust gas being measured in the preceding step side of above-mentioned reduction denitration treatment step; With the back step side of above-mentioned reduction denitration treatment step to above-mentioned waste gas in the mercury concentration determination step measured of the concentration of mercury; Based on the concentration of the above-mentioned nitrogen oxides of exhaust gas that obtains by above-mentioned nitrous oxides concentration determination step with by any side or both sides in the concentration of mercury in the above-mentioned waste gas of above-mentioned mercury concentration determination step acquisition, be adjusted at the quantity delivered of the above-mentioned reduction-oxidation auxiliary agent of supplying with in the above-mentioned reduction-oxidation auxiliary agent supplying step.
17) mercury of the waste gas of the 17th invention is removed method based on the 15th or the 16th invention; Between above-mentioned reduction-oxidation auxiliary agent supplying step and above-mentioned reduction denitration treatment step; Comprise any side or both sides in the hydrogen chloride gas supplying step of in above-mentioned flue, supplying with the ammonia supplying step of ammonia and in above-mentioned flue, supplying with hydrogen chloride gas; Based on the flow velocity of the above-mentioned waste gas that is gone out by above-mentioned flow measurement step measurements, any side in the above-mentioned hydrogen chloride gas of supplying with to the above-mentioned ammonia supplied with by above-mentioned ammonia supplying step, by above-mentioned hydrogen chloride gas supplying step perhaps adjust by both sides' spray amount, spray angle, initial velocity.
And,, can also adopt following formation in order to solve above-mentioned problem.
18) promptly; Can lean on back trip side that mixed organization is set than the zone of above-mentioned reduction-oxidation auxiliary agent generating gasification, above-mentioned oxidizing gas and above-mentioned reducibility gas that this mixed organization generates when being used to promote above-mentioned reduction-oxidation auxiliary agent generating gasification mix with above-mentioned waste gas.
19) compare with the supply position of supplying with above-mentioned reduction-oxidation auxiliary agent, above-mentioned mixed organization is arranged on the back trip side below the above 10m of 1m in the above-mentioned flue.
20) above-mentioned mixed organization forms by dispose the unit that a plurality of rotating flows that make above-mentioned waste gas produce rotating flow bring out parts according to the mode with the flow direction quadrature of above-mentioned waste gas.
21) above-mentioned mixed organization is provided with multistage said units at the flow direction of above-mentioned waste gas.
22) above-mentioned rotating flow brings out parts and has: a pair of the 1st rotating flow that has a subtend face at the entrance side of above-mentioned waste gas brings out plate and brings out plate at a pair of the 2nd rotating flow that the discharge side of above-mentioned waste gas has a subtend face; Bring out in the linking part that plate links above-mentioned the 1st rotating flow being brought out plate and above-mentioned the 2nd rotating flow, the subtend face that connects to both sides respectively is different.
23) above-mentioned rotating flow bring out width L, the height D of parts can scope for following formula in.
MIN(B、H)/10≤L≤MIN(B、H)…(5)
MIN(B、H)/10≤D≤5×MIN(B、H)…(6)
Wherein, B is the length that a limit in flue cross section in the position is set, and H is the length on another limit in flue cross section, and MIN (B, H) is the value of the length of any short brink among the length H on another limit in length B, flue cross section on a limit in flue cross section.
24) above-mentioned flue is leaning on the inwall of the above-mentioned flue of back trip side to be provided with protruding part spare than the supply position of in above-mentioned flue, supplying with above-mentioned reduction-oxidation auxiliary agent.
25) above-mentioned flue is leaning on back trip side to be provided with the contraction flow region that the path in the above-mentioned flue is narrowed down than the supply position of in above-mentioned flue, supplying with above-mentioned reduction-oxidation auxiliary agent.
26) on the guide vane of the upstream side that is arranged at above-mentioned reduction denitration mechanism, be provided with the above-mentioned reducibility gas that promotes after the gasification, the mixing that above-mentioned oxidizing gas mixes promotes accessory in above-mentioned waste gas.
27) above-mentioned spray nozzle can be to spray the two-fluid spray nozzle of the spraying of above-mentioned reduction-oxidation auxiliary agent, above-mentioned reduction-oxidation auxiliary agent with air.
28) leaning on upstream side, be provided with the flow rate-measuring device that the flow velocity of above-mentioned waste gas is measured than the supply position of supplying with above-mentioned reduction-oxidation auxiliary agent.
According to the present invention; In the flue of the reduction-oxidation auxiliary agent that generates oxidizing gas and reducibility gas when utilizing a plurality of spray nozzles to gasify with the liquid downstream that are sprayed to boiler; Above-mentioned spray nozzle supplies to this reduction-oxidation auxiliary agent in the above-mentioned flue according to the mode that does not make above-mentioned reduction-oxidation auxiliary agent be attached to the inwall of above-mentioned flue, and the oxidizing gas and the reducibility gas concentration stabilize that produce in the time of can the reduction-oxidation auxiliary agent being gasified thus supply in the flue equably.Therefore, not only can improve the oxidation susceptibility of mercury in the reduction denitrification apparatus, and can improve the reducing property of nitrogen oxide.
In addition, before gasification, be attached to the wall of above-mentioned flue, so the breakage of the above-mentioned flue that can prevent to take place because of the corrosion of above-mentioned flue etc. owing to can prevent above-mentioned reduction-oxidation auxiliary agent.
Description of drawings
Fig. 1 is the skeleton diagram of the formation of the emission-control equipment that relates to of expression embodiments of the invention 1.
Fig. 2 is to the NH from the spray nozzle spraying 4The figure that the spray angle of the relative flue of Cl solution describes.
Fig. 3 is expression NH 4The figure of an example of the formation of Cl solution feed mechanism.
Fig. 4 is the figure that specifically representes the formation of denitrification apparatus.
The figure of the section that Fig. 5 is expression when the flow direction of waste gas is observed the flue of the emission-control equipment that embodiments of the invention 2 relate to.
The figure of the section that Fig. 6 is expression when the flow direction of waste gas is observed the flue of the emission-control equipment that embodiments of the invention 3 relate to.
Fig. 7 is the figure of the formation of schematic representation spray nozzle.
Fig. 8 is the partial enlarged drawing of spray nozzle.
The figure of the section that Fig. 9 is expression when the flow direction of waste gas is observed the flue of the emission-control equipment that embodiments of the invention 4 relate to.
Figure 10 is the concept map of the formation of the emission-control equipment that relates to of schematic representation embodiments of the invention 5.
Figure 11 is the vertical view of an example of expression blender.
Figure 12 is the vertical view that the rotating flow of formation blender brings out parts.
Figure 13 is the front view that rotating flow brings out parts.
Figure 14 is the stereogram that rotating flow brings out parts.
Figure 15 is the figure of the gas flow of waste gas when schematically representing to be arranged on blender in the flue.
Figure 16 is the partial enlarged drawing of Figure 15.
Figure 17 is the NH in the waste gas when schematically representing not to be arranged at blender in the flue 3The figure of an example of CONCENTRATION DISTRIBUTION.
Figure 18 is the NH in the waste gas when schematically representing to be arranged at blender in the flue 3The figure of an example of CONCENTRATION DISTRIBUTION.
Figure 19 is the figure of relation of size of crushing and the blender of expression blender.
Figure 20 is the figure of the short side direction from flue of the emission-control equipment that relates to of embodiments of the invention 6 when observing.
Figure 21 is the figure when the long side direction of flue is observed.
Figure 22 is the figure of the short side direction from flue of the emission-control equipment that relates to of embodiments of the invention 7 when observing.
Figure 23 is the figure when the long side direction of flue is observed.
Figure 24 is the figure when the short side direction of flue is observed.
Figure 25 is the figure when the long side direction of flue is observed.
Figure 26 is the figure of the part of the emission-control equipment that relates to of expression embodiments of the invention 8.
Figure 27 is the local amplification stereogram of the part among Figure 26.
Figure 28 is the figure of the formation of the emission-control equipment that relates to of schematic representation embodiments of the invention 9.
Figure 29 is the figure of expression from the skeleton diagram of the exhaust treatment system of the waste gas of boiler discharge.
The figure of Figure 30 configuration of spray nozzle when the flow direction of the waste gas of flue is observed that is expression.
The specific embodiment
Below, with reference to accompanying drawing the present invention is elaborated.Need to prove that the present invention also can't help this embodiment and limits.And the inscape among the following embodiment comprises key element that those skilled in the art expect easily, or identical in fact key element.
[embodiment 1]
With reference to accompanying drawing, the emission-control equipment that embodiments of the invention 1 are related to describes.
Fig. 1 is the skeleton diagram of the formation of the emission-control equipment that relates to of expression embodiments of the invention 1.
Emission-control equipment 10 as shown in Figure 1, that present embodiment relates to is emission-control equipments that the nitrogen oxide (NOx) that contains in the waste gas 12 from boiler 11, mercury (Hg) are removed, and it has: ammonium chloride (NH 4Cl) solution feed mechanism (reduction-oxidation auxiliary agent feed mechanism) 16, it will contain ammonium chloride (NH through a plurality of spray nozzles 15 4Cl) as the ammonium chloride (NH of reduction-oxidation auxiliary agent 4Cl) solution 14 is with flue 13 internal sprayings in liquid downstream to boiler 11; Reduction denitrification apparatus (reduction denitration mechanism) 18, it has with ammonia (NH 3) the gas denitrating catalyst that as reducibility gas the NOx in the waste gas 12 reduced and Hg is carried out oxidation under as hydrogen chloride (HCl) gas coexistence of oxidizing gas; Heat exchanger (air heater) 19, its waste gas 12 after to denitration carries out heat exchange; Dust arrester 20, the coal dust in its waste gas 12 after with denitration is removed; With wet desulfurizer 22, it uses lime stone-gypsum slurry 21, and the Hg after will be in reduction denitrification apparatus 18 oxidized removes as the alkali absorption liquid.
In addition, in the emission-control equipment 10 that present embodiment relates to, used NH 4Cl is as the reduction-oxidation auxiliary agent, but the present invention is not limited thereto, and the reduction-oxidation auxiliary agent is so long as generate the auxiliary agent of oxidizing gas and reducibility gas and get final product when gasification.
In addition, in the present invention, the reduction-oxidation auxiliary agent is as being used for down in oxidizing gas coexistence mercury (Hg) to be carried out oxidation and the auxiliary agent of the reducing agent performance function of NOx being reduced with the oxidation promoter of its chlorination with through reducibility gas.In the present embodiment, use HCl gas, use NH as oxidizing gas 3Gas is as reducibility gas.
Utilize NH 4Cl solution feed mechanism 16 is supplied with NH to the waste gas of discharging from boiler 11 12 4Cl solution 14.NH 4Cl solution feed mechanism 16 contains spray nozzle 15.Spray nozzle 15 has NH 4Cl solution 14 is with the liquid ammonium chloride (NH that in flue 13, supplies with 4Cl) solution supply pipe 25 and will be in flue 13 compression spraying NH 4The air 26 of Cl solution 14 supplies to the air supply pipe 27 in the flue 13, is made up of two-fluid spray nozzle.Spray nozzle 15 has and is used for to ammonium chloride (NH 4Cl) leading section of solution supply pipe 25 and air supply pipe 27 sprays NH simultaneously 4The nozzle bore 15a of Cl solution 14 and air 26.
NH 4Cl solution 14 is at ammonium chloride (NH 4Cl) be adjusted to normal concentration in the NaOH solution tank NaOH 28.And, from NH 4The NH that Cl solution supply pipe 25 is supplied with 4The flow of Cl solution 14 is adjusted by valve V1.NH 4Cl solution 14 is from NH 4Cl NaOH solution tank NaOH 28 is at NH 4In the Cl solution supply pipe 25 through and by spray nozzle 15 to flue 13 internal sprayings.
To NH 4Cl solution feed mechanism 16 is configured to spray nozzle 15 according to NH 4Cl solution 14 is not attached to the mode of inwall 13a (with reference to Fig. 2) of the flue 13 of waste gas 12 circulation and supplies with NH 4Cl solution 14.As according to not making NH 4Cl solution 14 is attached to the mode of inwall 13a of the flue 13 of waste gas 12 circulation and supplies with NH 4The configuration of Cl solution 14, preferably spray nozzle 15 separates the structure that the distance more than certain is configured with the inwall 13a of flue 13 in flue 13.Certain above distance is meant the NH that is sprayed 4Enough distances of the drop of Cl solution 14 generating gasification before the inwall 13a that arrives flue 13 from the nozzle bore of spray nozzle 15.If consider the treatment conditions of actual flue size, reality, the wall that the nozzle bore of preferred spray nozzle 15 for example is arranged on apart from flue 13 is the position more than the 0.5m.
Position and the wall of flue 13 of the nozzle bore of spray nozzle 15 are apart from the reason more than the 0.5m, need to consider the gas flow rate of waste gas 12, from the NH of spray nozzle 15 sprayings 4The drop initial velocity of Cl solution 14, liquid-drop diameter, from the NH of spray nozzle 15 sprayings 4Spray angle, the EGT of waste gas 12, the NH of Cl solution 14 relative flues 13 4The drop temperature of Cl solution 14 etc.As an one of which example, can specifically determine as described below.
That is, the gas flow rate of the waste gas in flue 13 12 be about 15m/s, from the NH of spray nozzle 15 sprayings 4The drop initial velocity of Cl solution 14 is about 300m/s, the gas temperature of waste gas 12 is about 350 ℃, NH 4The drop temperature of Cl solution 14 is under the situation about 20 ℃, according to NH 4The NH that the liquid-drop diameter of Cl solution 14 is inferred 4The drop of Cl solution 14 is from being sprayed to time and the NH till the evaporation 4The displacement that the drop of Cl solution 14 arrives till the evaporation is different.
Represented NH in the table 1 4The liquid-drop diameter of Cl solution 14, drop are from being sprayed to an example of the relation time till the evaporation, the drop displacement till the evaporation.In table 1, t representes NH 4The drop of Cl solution 14 is from being sprayed to the time till the evaporation, and l representes the displacement till drop arrives evaporation.
[table 1]
Figure BDA0000133787650000101
As shown in table 1, at NH 4When the liquid-drop diameter of Cl solution 14 was the 40 μ m left and right sides, calculating this drop was about 0.032s from the time t that is sprayed to till the evaporation, NH 4The displacement l of the drop of Cl solution 14 till the evaporation from spray nozzle 15 with mobile parallel being oriented about 0.76m of waste gas 12.In addition, at NH 4When the liquid-drop diameter of Cl solution 14 was the 60 μ m left and right sides, calculating this drop was about 0.068s from the time t that is sprayed to till the evaporation, NH 4The displacement l of the drop of Cl solution 14 till the evaporation from spray nozzle 15 with mobile parallel being oriented about 1.6m of waste gas 12.In addition, at NH 4When the liquid-drop diameter of Cl solution 14 was the 80 μ m left and right sides, calculating this drop was about 0.119s from the time t that is sprayed to till the evaporation, NH 4The drop of Cl solution 14 to the evaporation till displacement l be about 2.7m from spray nozzle 15 in spray direction.
Next, research is from the NH of spray nozzle 15 sprayings 4The spray angle of Cl solution 14 relative flues 13.Fig. 2 is the NH of explanation from the spray nozzle spraying 4The figure of the spray angle of the relative flue of Cl solution.In Fig. 2, the NH that will spray from the nozzle bore 15a of spray nozzle 15 4The spray angle of the wall of the relative flue 13 of the drop of Cl solution 14 is made as α, and the beeline till will be from the inwall 13a of flue 13 to the nozzle bore 15a of spray nozzle 15 is made as x.
As shown in Figure 2, through the NH that sprays according to nozzle bore 15a from spray nozzle 15 4The spray angle α of the wall of the relative flue 13 of the drop of Cl solution 14 is provided with spray nozzle 15 according to the mode that satisfies following formula (1), can make from the drop of spray nozzle 15 spraying not with the wall collision of flue 13.
l×sinα＜x…(1)
Wherein, l representes NH 4The drop of Cl solution arrives the displacement till the evaporation.
Illustrated in the table 2 from the NH of the nozzle bore 15a spraying of spray nozzle 15 4The spray angle α of the wall of the relative flue 13 of the drop of Cl solution 14, when being 10 ° of left and right sides with respect to the gas flow direction of waste gas 12, the example of the beeline x till from the inwall 13a of flue 13 to the nozzle bore 15a of spray nozzle 15.
[table 2]
Figure BDA0000133787650000121
As shown in table 2, at NH 4When the liquid-drop diameter of Cl solution 14 was the 40 μ m left and right sides, the beeline x till from the inwall 13a of flue 13 to the nozzle bore 15a of spray nozzle 15 was about 0.13m.In addition, at NH 4When the liquid-drop diameter of Cl solution 14 was the 60 μ m left and right sides, the beeline x till from the inwall 13a of flue 13 to the nozzle bore 15a of spray nozzle 15 was about 0.28m.In addition, at NH 4When the liquid-drop diameter of Cl solution 14 was the 80 μ m left and right sides, the beeline x till from the inwall 13a of flue 13 to the nozzle bore 15a of spray nozzle 15 was about 0.47m.
Therefore, the NH that sprays as nozzle bore 15a from spray nozzle 15 4The spray angle α of the wall of the relative flue 13 of the drop of Cl solution 14 is when being 10 ° of left and right sides with respect to the gas flow direction of waste gas 12, at NH 4The liquid-drop diameter of Cl solution 14 is under the situation about 40 μ m, need the nozzle bore 15a of spray nozzle 15 be arranged to apart from flue 13 to more than the 0.13m.In addition, at NH 4The liquid-drop diameter of Cl solution 14 is under the situation about 60 μ m, need the nozzle bore 15a of spray nozzle 15 be arranged to apart from flue 13 to more than the 0.28m.In addition, at NH 4The liquid-drop diameter of Cl solution 14 is under the situation about 80 μ m, need the nozzle bore 15a of spray nozzle 15 be arranged to apart from flue 13 to more than the 0.47m.
Therefore, for example to be set at the wall apart from flue 13 be the position more than the 0.5m to the nozzle bore 15a of spray nozzle 15.Thus, about the position of the nozzle bore 15a of spray nozzle 15, become gas flow rate corresponding to waste gas 12, from the NH of the nozzle bore 15a spraying of spray nozzle 15 4The drop initial velocity of Cl solution 14, liquid-drop diameter, from the NH of spray nozzle 15 sprayings 4Spray angle, the EGT of waste gas 12, the NH of Cl solution 14 relative flues 13 4The drop temperature of Cl solution 14 etc., the NH that is sprayed 4The drop of Cl solution 14 arrives enough distances of generating gasification before the inwall 13a of flues 13 from spray nozzle 15.Its result, spray nozzle 15 can be according to NH 4Cl solution 14 is not attached to the mode of inwall 13a of the flue 13 of waste gas 12 circulation and in flue 13, supplies with NH 4Cl solution 14.
As above-mentioned, spray nozzle 15 is by spraying NH simultaneously 4 Cl solution 14 constitutes with the two-fluid spray nozzle of the air 26 of compression usefulness.Air 26 is transferred to spray nozzle 15 via air supply pipe 27 from air supply unit 31, as the NH that spray from spray nozzle 15 4Compression during Cl solution 14 is used with air.The NH that can will spray from spray nozzle 15 through air 26 thus, 4 Cl solution 14 becomes small drop and is sprayed in the flue 13.
The flow of the air of supplying with from air supply pipe 27 in addition, 26 is adjusted by valve V2.Based on the flow of the air of supplying with from air supply pipe 27 26, can adjust from the NH of spray nozzle 15 sprayings 4The drop size of Cl solution 14.
The flow of the air 26 that preferably will spray from spray nozzle 15 in addition, for example is made as gas-water ratio more than 100 (volume ratio) below 10000.This is because make the NH that sprays from spray nozzle 15 4 Cl solution 14 becomes small drop and is sprayed in the flue 13.
NH 4Cl solution feed mechanism 16 utilizes spray nozzle 15, from spray nozzle 15 with NH 4Cl solution 14 is to flue 13 internal sprayings, but the present invention is not limited thereto.NH 4Cl solution feed mechanism 16 is so long as can be with NH 4Cl solution 14 stably gets final product to the mechanism of flue 13 internal sprayings.Fig. 3 is expression NH 4The figure of an example of the formation of Cl solution feed mechanism.As shown in Figure 3, NH 4Cl solution feed mechanism 16 becomes with NH spray nozzle 15 4Cl solution supply pipe 25 is as interior pipe, with the dual pipe structure of air supply pipe 27 as outer tube, and is provided with nozzle bore 15a at the leading section of nozzle bore 15a.Owing to surround NH through spray nozzle 15 being constituted air supply pipe 27 4Cl solution supply pipe 25, and spray nozzle 15 is inserted in the flue 13, air 26 can be at NH 4Flow between Cl solution supply pipe 25 and the air supply pipe 27, passed to NH by air 26 so can prevent the heat of the waste gas 12 in the flue 13 4Cl solution 14.Therefore, owing to can prevent NH 4Cl solution 14 is by the heating of the heat of waste gas 12, so NH 4Cl solution 14 can be kept liquid condition before being sprayed.
And, NH 4Cl solution feed mechanism 16 has: according to the mode of in flue 13, surrounding spray nozzle 15 be inserted into flue 13 in being blown into pipe 32 and to being blown into the air supply pipe 34 of managing air supply 33 in 32.In addition, the nozzle bore 15a of spray nozzle 15 is arranged at the spray-hole 35 of the wall that is blown into pipe 32.
Air 33 is used to make NH 4The drop of Cl solution 14 further disperses in flue 13.Air 33 is transferred to being blown into pipe 32 via air supply pipe 34 from air supply unit 36, from slit 37 injections between the nozzle bore 15a that is blown into pipe 32 spray-hole 35 and spray nozzle 15.Through 37 injection airs 33, can make from the NH of spray nozzle 15 sprayings from the slit 4The drop of Cl solution 14 disperses in flue 13.In addition, as shown in Figure 1, the flow of the air of supplying with from air supply unit 36 33 is adjusted by valve V3.
In addition, air 33 is used to prevent the NH from spray nozzle 15 sprayings 4The NH of Cl solution 14 4The temperature that are blown in pipe 32 and the inhibition spray nozzle 15 that are attached to Cl rise and prevent NH 4Separating out of the boiling of Cl solution 14 and ammonium chloride particle.As shown in Figure 3, be inserted in the flue 13 according to the mode of surrounding spray nozzle 15 owing to be blown into pipe 32, air 33 is being blown into the NH of pipe 32 with spray nozzle 15 4Flow between the Cl solution supply pipe 25, so air 33 is as NH 4The tempering air performance function of Cl solution 14.Thereby, can prevent that the heat of the waste gas 12 in the flue 13 is delivered to the NH of spray nozzle 15 from the outside that is blown into pipe 32 4In the Cl solution supply pipe 25.Therefore, rise, take precautions against NH through preventing the temperature in the spray nozzle 15 4 Cl solution 14 is heated, and can prevent NH 4Cl solution 14 seethes with excitement in spray nozzle 15, can make NH 4Cl solution 14 was kept liquid condition before being sprayed.In addition, can also prevent the corrosion of spray nozzle 15.
In addition, rise, can use metal material as constituting NH in order to prevent the temperature in the spray nozzle 15 4The material of Cl solution supply pipe 25, air supply pipe 27.As constituting NH 4The material of Cl solution supply pipe 25, air supply pipe 27 is for example for NH 4Cl solution supply pipe 25 can be enumerated nickel base heat resistant-corrosion resisting alloy, resin-lined steel pipes (low temperature portion) such as corrosion resistant metal, for example Hasiteluoyi C.For air supply pipe 27, can enumerate carbon steel, stainless steel etc.
In addition, spray nozzle 15 is for NH 4The spraying of Cl solution 14 with and used two-fluid spray nozzle, but the present invention is not limited thereto, and also can use the single fluid nozzle of common liquid spraying usefulness.
In addition, because spray nozzle 15 becomes NH 4Cl solution supply pipe 25 is constructed with the dual pipe of air supply pipe 27, and has surrounded NH by air supply pipe 27 4Around the Cl solution supply pipe 25, so can prevent NH 4Cl solution 14 is blown into pipe 32 by the heating of the heat of waste gas 12 through around spray nozzle 15, being provided with, and can prevent NH more reliably 4 Cl solution 14 is heated by the heat of waste gas 12.
NH 4Cl solution supply pipe 25 is set in the air supply pipe 27, but NH 4Cl solution supply pipe 25 also can not be arranged in the air supply pipe 27 and be arranged on the outside of air supply pipe 27.
In addition, from air supply unit 31 air supplies 26, from air supply unit 36 air supplies 33, by respectively different supply source air supplies, but the present invention is not limited thereto, also can be from same supply source air supply.That is, air 33 can use the air of supplying with from air supply unit 31.In addition, air 26 can use the air of supplying with from air supply unit 36.
In addition, be sprayed to the NH in the flue 13 by spray nozzle 15 4The drop of Cl solution 14 through the high-temperature atmosphere temperature evaporation based on waste gas 12, and generates small NH 4The solids of Cl resolve into HCl and NH as shown in the formula (2) that kind 3And distil.Therefore, through the NH that spray from spray nozzle 15 4 Cl solution 14 can be by the NH that is sprayed 4The drop of Cl solution 14 produces HCl, NH 3, with NH 3Gas, HCl gas supply in the flue 13.
NH 4Cl→NH 3+HCl…(2)
In addition, the temperature of the waste gas 12 in the flue 13 for example is more than 320 ℃ below 420 ℃, is high temperature.The NH of spray nozzle 15 4Cl solution supply pipe 25 is arranged on and is blown in the pipe 32, and air 33 is used to make NH 414 coolings of Cl solution.Therefore, through NH before being sprayed by spray nozzle 15 4 Cl solution 14 keeps liquid condition, from spray nozzle 15 with NH 4Cl solution 14 can make the NH of ejection based on the high-temperature atmosphere temperature of waste gas 12 with the droplet-like spraying 4The droplets vaporize of Cl solution 14.
In addition, the NH that preferably sprays from spray nozzle 15 4Fine droplet below the above 100 μ m of the liquid-drop diameter average out to 1nm of Cl solution 14.Through generating the fine droplet below the 100 μ m more than the average out to 1nm, can be with NH from being sprayed 4The NH that the drop of Cl solution 14 produces 4The solids of Cl resolve into NH to lack the holdup time in waste gas 12 3, HCl and make its distillation.Thus, owing to do not need to heat in advance NH 4Cl solution 14 is so can prevent flue 13, rudimentaryization of spray nozzle 15, corrosion.
NH 4Cl solution 14 can be through making ammonium chloride (NH 4Cl) powder dissolution generates in water.Through adjustment NH 4Cl powder, water quantity delivered separately can be adjusted the NH of normal concentration 4Cl solution 14.NH 4Cl solution 14 also can pass through HCl solution and NH 3Solution generates with the mixed of normal concentration.
In addition, for example under the temperature of drop is 20 ℃ situation, preferred NH 4The concentration of Cl solution 14 is below the above 30wt% of 20wt%.Table 3 illustrates NH 4Relation between the temperature of the drop of Cl solution 14, solubility, the concentration.As shown in table 3, NH 4The solubility of Cl solution 14 roughly determines according to the temperature of drop.
[table 3]
Figure BDA0000133787650000161
In addition, the temperature of the waste gas 12 in the flue 13 also depends on the burning condition of boiler 11, for example is preferably more than 320 ℃ below 420 ℃, more preferably more than 320 ℃ below 380 ℃, and then is preferably more than 350 ℃ below 380 ℃.Its reason is, in these temperature bands, the oxidation reaction of denitration reaction and the Hg of NOx can take place on denitrating catalyst efficiently simultaneously.
Therefore, because through by the NH of spray nozzle 15 according to mode feed fluid state in flue 13 of the inwall 13a that is not attached to flue 13 4 Cl solution 14, the high-temperature atmosphere temperature of can concentration stabilize in flue 13, supplying with through waste gas 12 equably makes NH 4HCl gas, NH after Cl solution 14 decomposes 3Gas is so can make HCl gas, the NH in the waste gas 12 3The CONCENTRATION DISTRIBUTION of gas is even.In addition, owing to can prevent NH 4Cl solution 14 was attached to the wall of flue 13 before gasification, so the breakage of the flue 13 that can prevent to take place because of the corrosion of flue 13 etc.
In addition, by NH 4HCl gas, NH that the drop of Cl solution 14 produces 3Gas is as shown in Figure 1, is accompanied by waste gas 12 and is together flowed to reduction denitrification apparatus 18.Fig. 4 is the figure that specifically representes the formation of denitrification apparatus.As shown in Figure 4, reduction denitrification apparatus 18 is made up of 3 denitrating catalyst layer 38-1～38-3.And waste gas 12 is making gas flow even through the effect of cowling panel 39 through reduction denitrification apparatus 18 before.NH 4Cl decomposes and the NH of generation 3Gas is used to the reduction denitration of NOx in reduction denitrification apparatus 18, HCl gas is used to the oxidation of Hg, thereby NOx and Hg are removed from waste gas 12.
That is, on the denitrating catalyst of the denitrating catalyst layer 38-1～38-3 that is filled into reduction denitrification apparatus 18, NH 3As shown in the formula (3) are such NOx is reduced denitration, HCl carries out mercury oxidation as shown in the formula (4) are such to Hg.
4NO+4NH 3+O 2→4N 2+6H 2O…(3)
Hg+1/2O 2+2HCl→HgCl 2+H 2O…(4)
In addition, reduction denitrification apparatus 18 is made up of 3 denitrating catalyst layer 38-1～38-3, but the present invention is not limited thereto, and reduction denitrification apparatus 18 can suitably change the quantity of denitrating catalyst layer corresponding to denitration performance.
And as shown in Figure 1, after the oxidation of the reduction of in reduction denitrification apparatus 18, having carried out the NOx in the waste gas 12 and Hg, waste gas 12 is transferred to wet type desulfurizer 22 through air heater 19, dust arrester 20.In addition, can between air heater 19 and dust arrester 20, heat regenerator be set.
In wet desulfurizer 22, the side surface side of the bottom in the apparatus main body 41 is carried waste gas 12, utilizes absorption liquid pipeline 42 to supply in the apparatus main body 41 as the lime stone-gypsum slurry 21 that the alkali absorption liquid uses, through nozzle 43 towards top of tower side jet flow.Make bottom sides in the apparatus main body 41 rise the waste gas 12 that comes, the lime stone-gypsum that flows down with spraying from nozzle 43 starches 21 subtends and gas-liquid contacts; Make HgCl, oxysulfide (SOx) in the waste gas 12 be absorbed in the lime stone-gypsum slurry 21 and separate, remove, thereby waste gas 12 is cleaned from waste gas 12.By the waste gas 12 after 21 purifications of lime stone-gypsum slurry, discharged from the top of tower side as Purge gas 44, be discharged to outside the system from chimney 45 then.
The employed lime stone-gypsum slurry 21 of the desulfurization of waste gas 12 is dissolved in the lime white CaCO that water obtains through making limestone powder 3, the SOx reaction in lime and the waste gas 12 so carry out oxidation after calcium plaster CaSO 4, mix with water and generate.Lime stone-gypsum slurry 21 for example can be extracted the liquid that the tower bottom 55 at the apparatus main body 41 of wet desulfurizer 22 stockpiles out and use.In apparatus main body 41, the such reaction of following formula (5) takes place in SOx in the waste gas 12 and lime stone-gypsum slurry 21.
CaCO 3+SO 2+0.5H 2O→CaSO 3·0.5H 2O+CO 2…(5)
On the other hand, absorbed the lime stone-gypsum slurry 21 behind the SOx in the waste gas 12, mixed with water 46 in being fed into apparatus main body 41, the air 47 that the tower bottom 55 through apparatus main body 41 is supplied to carries out oxidation processes.The such reaction of following formula (6) takes place with water 46, air 47 in the lime stone-gypsum slurry 21 that in apparatus main body 41, flows down at this moment.
CaSO 3·0.5H 2O+0.5O 2+1.5H 2O→CaSO 4·2H 2O…(6)
In addition; The lime stone-gypsum slurry 21 that is used for desulfurization that the tower bottom 55 of wet desulfurizer 22 stockpiles is after oxidized processing; Take out and be transported to dehydrator 48 from tower bottom 55, be discharged to outside the system as the dehydration grumeleuse (gypsum) 49 that contains mercury chloride (HgCl) then.As dehydrator 48, for example can use belt filter etc.In addition, the filtrating after the dehydration (dehydration filtrating) for example is carried out the outstanding absurd creature in the dehydration filtrating, the drainings such as pH adjustment of filtrating of removing, dewater of heavy metal are handled.The part of the dehydration filtrating after this draining is handled is sent back in the wet desulfurizer 22, and another part of dehydration filtrating is processed as draining.
The HgCl in can absorbing waste gas 12 in addition, used lime stone-gypsum slurry 21, as long as but also can use other solution as the alkali absorption liquid as the alkali absorption liquid.
Be not limited to lime stone-gypsum slurry 21 from the method for nozzle 43 towards top of tower side jet flow, for example also can from nozzle 43 and waste gas 12 subtends flow down.
<nH 4The Kong Zhi > of the spray amount of Cl solution;
At the upstream side of spray nozzle 15, be provided with the flowmeter 51 that the flow of waste gas 12 is carried out instrumentation.Measure the flow of waste gas 12 through flowmeter 51.The flow value of the waste gas 12 that is determined by flowmeter 51 is sent out to control device 52, can adjust the NH that sprays from spray nozzle 15 based on the flow value of waste gas 12 4The flow of Cl solution 14, angle, initial velocity etc.
And, be provided with NOx densimeter 53 at the outlet side of wet desulfurizer 22.The value of NOx concentration is delivered to control device 52 in the Purge gas 44 that is determined by NOx densimeter 53.Control device 52 can confirm to reduce the reduction ratio of the NOx in the denitrification apparatus 18 according to the value of the NOx concentration in the Purge gas that is determined by NOx densimeter 53 44.Therefore, through controlling NH according to the value of the NOx concentration in the Purge gas 44 that determines by NOx densimeter 53 4The NH of Cl solution 14 4Cl concentration, supply flow rate etc. can make from the NH of spray nozzle 15 sprayings 4The NH of Cl solution 14 4Cl concentration satisfies the denitration performance of regulation.
In addition, in flue 13, be provided with mercury (Hg) densimeter 54-1, the 54-2 that the Hg content the waste gas 12 of discharging from boiler 11 is measured.Hg densimeter 54-1 is arranged in the flue 13 between boiler 11 and the spray nozzle 15, and Hg densimeter 54-2 is arranged between reduction denitrification apparatus 18 and the heat exchanger 19.The value of the Hg concentration in the waste gas 12 that is determined by Hg densimeter 54-1,54-2 is delivered to control device 52.The content of the Hg that control device 52 can be confirmed to contain in the waste gas 12 according to the value of the Hg concentration in the waste gas 12 that is determined by Hg densimeter 54-1,54-2.Through controlling NH according to the value of the Hg concentration in the waste gas 12 that determines by Hg densimeter 54-1,54-2 4The NH of Cl solution 14 4Cl concentration, supply flow rate can make from the NH of spray nozzle 15 sprayings 4The NH of Cl solution 14 4Cl concentration, supply flow rate satisfy the denitration performance of regulation, and can keep the oxidation susceptibility of Hg.
In addition, at the tower bottom 55 of wet desulfurizer 22, be provided with the oxidation reduction potential determination control device (ORP controller) 56 that the oxidation-reduction potential of lime stone-gypsum slurry 21 is measured.Measure the value of the oxidation-reduction potential of lime stone-gypsum slurry 21 through this ORP controller 56.Based on the value of the oxidation-reduction potential that determines, the quantity delivered of the air 47 that the tower bottom 55 of subtend wet desulfurizer 22 is supplied with is adjusted.Through the quantity delivered of the air 47 that is supplied to of adjustment tower bottom 55, can prevent to be trapped in the lime stone-gypsum slurry 21 that the tower bottom 55 of wet desulfurizer 22 stockpiles oxidized after the Hg reduction, and prevent from chimney 45 diffusions.
In order to prevent that Hg from dispersing from lime stone-gypsum slurry 21 again, the oxidation-reduction potential of the lime stone-gypsum slurry 21 in the preferred wet desulfurizer 22 for example is positioned at the scope below the above 600mV of 150mV.Its reason is, if oxidation-reduction potential in above-mentioned scope, then is as HgCl in lime stone-gypsum slurry 21 2And the stable zone of the Hg that is captured can prevent Hg dispersing again in atmosphere.
In addition, in the emission-control equipment 10 that present embodiment relates to, used NH 4Cl is as the reduction-oxidation auxiliary agent, but also can adopt NH 4Ammonium bromide (NH beyond the Cl 4Br), ammonium iodide (NH 4I) etc. ammonium halide uses it is dissolved in the solution of water as the reduction-oxidation auxiliary agent.
Like this, the emission-control equipment 10 that relates to according to present embodiment is because NH 4Cl solution feed mechanism 16 is supplied with NH according to the mode of the inwall 13a of the flue 13 that is not attached to waste gas 12 circulations from spray nozzle 15 4 Cl solution 14 is so can make the NH that is sprayed in the flue 13 4The droplets vaporize of Cl solution 14 and the HCl, the NH that generate 3Mix with waste gas 12.Therefore, since can concentration stabilize stable supplying HCl, NH in flue 13 equably 3So, can improve the oxidation susceptibility of Hg in the reduction denitrification apparatus 18, and the reducing property of NOx is improved.In addition, owing to can prevent NH 4Cl solution 14 was attached to the wall of flue 13 before gasification, so the breakage of the flue 13 that can also prevent to take place because of the corrosion of flue 13 etc. etc.
[embodiment 2]
With reference to accompanying drawing, the emission-control equipment that embodiments of the invention 2 are related to describes.Because the emission-control equipment that embodiments of the invention 2 relate to is identical with the formation of the emission-control equipment 10 that embodiments of the invention 1 shown in Figure 1 relate to, so only use the figure of the formation of the injection nozzle in the expression flue to describe in the present embodiment.The figure of the section that Fig. 5 is expression when the flow direction of waste gas is observed the flue of the emission-control equipment that embodiments of the invention 2 relate to.Wherein, give same Reference numeral for the parts of the formation repetition of the emission-control equipment that relates to embodiment 1, and omit its explanation.
As shown in Figure 5, the emission-control equipment that present embodiment relates to constitutes through a plurality of spray nozzles 15 are configured in the flue 13 according to the mode that satisfies following formula (7).
a≤b/5…(7)
Wherein, a is the nozzle distance between borehole of the nozzle bore of spray nozzle, and b is the length of long side in the length in flue cross section.
Owing to, can in flue 13, supply with NH according to the mode of the inwall 13a that is not attached to flue 13 from spray nozzle 15 through a plurality of spray nozzles 15 being configured in the flue 13 according to the mode that satisfies above-mentioned formula (7) 4 Cl solution 14, and make the quantity of the spray nozzle 15 that is provided with in the flue 13 more than in the past, so can in flue 13, dispose spray nozzle 15 rightly.Therefore, be sprayed to NH in the waste gas 12 owing to making 3, HCl amount is more, so can promote NH 3Gas, the mixing of HCl gas in waste gas 12.
In addition, preferably a plurality of spray nozzles 15 are configured in the flue 13 according to the mode that satisfies following formula (8).
a≤b/10…(8)
Thereby the emission-control equipment according to present embodiment relates to owing to through according to the mode that satisfies above-mentioned formula (7) a plurality of spray nozzles 15 being configured in the flue 13, can increase NH 3Gas, the quantity delivered of HCl gas in waste gas 12, and reduce HCl gas, the NH in the flue 13 3The concentration deviation of gas, thus the oxidation susceptibility of Hg in the reduction denitrification apparatus 18 not only can further be improved, but also can further improve the reducing property of NOx.
[embodiment 3]
With reference to accompanying drawing, the emission-control equipment that embodiments of the invention 3 are related to describes.Because the emission-control equipment that embodiments of the invention 3 relate to is identical with the formation of the emission-control equipment 10 that embodiments of the invention 1 shown in Figure 1 relate to, so only use the figure of the formation of the injection nozzle in the expression flue to describe in the present embodiment.The figure of the section that Fig. 6 is expression when the flow direction of waste gas is observed the flue of the emission-control equipment that embodiments of the invention 3 relate to, Fig. 7 is the figure of the formation of schematic representation spray nozzle.Wherein, give same Reference numeral for the parts of the formation repetition of the emission-control equipment that relates to embodiment 1,2, and omit its explanation.
Like Fig. 6, shown in 7, in the emission-control equipment that present embodiment relates to, spray nozzle 61 is provided with 4 spraying NH 4The nozzle bore 15a of Cl solution 14.Owing to, can make from the NH of 1 spray nozzle 61 to flue 13 internal sprayings through increasing the nozzle bore 15a of spray nozzle 61 4The amount of Cl solution 14 increases, so can further promote HCl gas, NH 3The mixing of gas in waste gas 12.Therefore, in reduction denitrification apparatus 18, the oxidation susceptibility of Hg, the reducing property of NOx are further improved.
In addition, 15a interval c each other in preferred nozzle hole is below the 0.3m.Be assumed to be under the situation about 40 μ m at drop, can know according to table 2, the displacement of the horizontal direction of drop (that is the beeline x till, from the inwall 13a of flue 13 to the nozzle bore 15a of spray nozzle 15) is 0.13m.Because drop flows along gas flow direction after evaporation, distillation, so, hope the drop coincidence of spraying from 2 nozzle bore 15a before in evaporation-distillation for the homogenising of CONCENTRATION DISTRIBUTION.Fig. 8 illustrates the partial enlarged drawing of spray nozzle 61.As shown in Figure 8, the drop interval sum that along continuous straight runs advances before evaporation that sprays from 2 nozzle bore 15a is 0.26m (=0.13 * 2).Therefore, through nozzle bore 15a interval c each other is made as below the 0.3m, can make from the drop of 2 nozzle bore 15a ejections to overlap.In addition; The liquid-drop diameter that reality is adopted is from relation controlled, plant bulk; Adopting drop mostly is the liquid-drop diameter below the above 80 μ m of 40 μ m; Lower limit at this liquid-drop diameter is under the situation about 40 μ m, through nozzle bore 15a interval c each other is made as below the 0.3m, can make from the drop of 2 nozzle bore 15a sprayings to overlap each other.
In addition, in the emission-control equipment that present embodiment relates to, each spray nozzle 61 is provided with 4 nozzle bore 15a, but the present invention is not limited thereto, and also can be provided with 2,3 or more than 5.
[embodiment 4]
With reference to accompanying drawing, the emission-control equipment that embodiments of the invention 4 are related to describes.Because the emission-control equipment that embodiments of the invention 4 relate to is identical with the formation of the emission-control equipment 10 that embodiments of the invention 1 shown in Figure 1 relate to, so only use the figure of the formation of the injection nozzle in the expression flue to describe in the present embodiment.When in flue 13, being provided with 24 spray nozzles 15, the emission-control equipment that embodiments of the invention 4 relate to can change the spray amount from each spray nozzle 15-11～15-24.The figure of the section that Fig. 9 is expression when the flow direction of waste gas is observed the flue of the emission-control equipment that embodiments of the invention 4 relate to.Wherein, give same Reference numeral for the parts of the formation repetition of the emission-control equipment that relates to embodiment 1 to 3, and omit its explanation.
As shown in Figure 9; In the emission-control equipment that present embodiment relates to; Make the spray amount of the spray nozzle 15-1 that is provided with at the short brink of flue 13,15-11～15-13,15-23,15-24, the spray nozzle 15-2～15-10 that is provided with than the long side at flue 13, the spray amount of 15-14～15-22 are many.For example, be made as 1 o'clock in the spray amount with spray nozzle 15-2～15-10,15-14～15-22, the spray amount of spray nozzle 15-1,15-11～15-13,15-23,15-24 is 1.5.
Through making the NH that is sprayed at spray nozzle 15-1,15-11～15-13,15-23, the 15-24 of the short brink setting of flue 13 4The spray amount of Cl solution 14, the NH that is sprayed than spray nozzle 15-2～15-10,15-14～15-22 in the long side setting of flue 13 4The spray amount of Cl solution 14 is many, can be with NH 4Cl solution 14 is sprayed to the end of flue 13 efficiently.Therefore, can be with HCl gas, NH 3Gas supplies near the waste gas 12 that the end of flue 13, flows, and in reduction denitrification apparatus 18, can further improve the oxidation susceptibility of Hg, the reducing property of NOx.
In addition; In the emission-control equipment that present embodiment relates to; In the time will being made as 1 in the spray amount of the spray nozzle 15-2～15-10 of the long side setting of flue 13,15-14～15-22; Spray amount at the spray nozzle 15-1 of the short brink setting of flue 13,15-11～15-13,15-23,15-24 is 1.5, but the present invention is not limited thereto.The ratio of the spray nozzle that is provided with at the short brink of flue 13, the spray nozzle that is provided with long side at flue 13 can be according to the NOx concentration in the waste gas 12, Hg concentration, NH 4The spray amount of Cl solution 14 etc. are adjustment suitably.
In the emission-control equipment that present embodiment relates to, in flue 13, be provided with 24 spray nozzle 15-11～15-24, but the present invention is not limited thereto, also can a plurality of spray nozzles be set according to the area etc. of being provided with in the flue 13.
[embodiment 5]
With reference to accompanying drawing, the emission-control equipment that embodiments of the invention 5 are related to describes.Figure 10 is the concept map of the formation of the emission-control equipment that relates to of schematic representation embodiments of the invention 5.Wherein, because the formation of the emission-control equipment 10 that the emission-control equipment that relates to of present embodiment and embodiment 1 shown in Figure 1 relate to is identical, thus give same Reference numeral to same parts, and the explanation of omission repetition.
Shown in figure 10, the emission-control equipment 70 that present embodiment relates to has blender (mixed organization) 71, this blender 71 be provided with the NH of flue 13 of the emission-control equipment 10 that relates to than above-mentioned embodiment 1 shown in Figure 1 4Back trip side is leaned in the zone of Cl generating gasification, promotes to make NH 4The hydrogen chloride that is generated during the Cl generating gasification (HCl) gas and as the ammonia (NH of reducibility gas as oxidizing gas 3) gas mixes with waste gas 12.
Waste gas 12 is containing by NH 4The NH of Cl solution feed mechanism 16 sprayings 4HCl gas, the NH that drop produced of Cl solution 14 3After the gas, be transported to blender 71.Through utilizing 71 pairs of waste gas 12 of blender to stir, can promote HCl gas, NH 3The mixing of gas in waste gas 12 can make HCl gas, NH in the waste gas 12 3The CONCENTRATION DISTRIBUTION of gas is even.
The blender 71 of present embodiment and the NH that sprays out from spray nozzle 15 4The zone of Cl solution 14 generating gasification is compared and is arranged on back trip side.Under general equipment operation condition, preferred blender 71 and supply NH 4The supply position of Cl solution 14 is compared and is arranged on the above back trip side of 1m.Its reason is, under the equipment operation condition of reality, if blender 71 is apart from NH 4The supply position of Cl solution 14 is less than 1m, then NH 4The situation that the drop of Cl solution 14 contacted with blender 71 before generating gasification is more.Therefore, through with supply with NH 4The supply position of Cl solution 14 is compared blender 71 is arranged on the back trip side more than the 1m, can further promote HCl gas, NH 3Gas is to the mixing of waste gas 12.In addition, from the equipment configuration viewpoint of reality, blender 17 is apart from NH 4About the supply position 10m of Cl solution 14 is the upper limit.
In addition, Figure 11～Figure 14 illustrates the formation of blender 71.Figure 11 is the vertical view of an example of expression blender, and Figure 12 is the vertical view that the rotating flow of formation blender brings out parts, and Figure 13 is the front view that rotating flow brings out parts, and Figure 14 is the stereogram that rotating flow brings out parts.Wherein, in Figure 11～Figure 14,, Reference numeral 73 has been applied hachure for clear and definite different with the parts of Reference numeral 74.
Shown in figure 11, the blender 71 of present embodiment forms by disposed the unit that 6 rotating flows that make waste gas 12 produce rotating flows bring out parts 72 according to the mode with the flow direction quadrature of waste gas 12.Like Figure 12～shown in Figure 14; Rotating flow brings out parts 72 to have: a pair of the 1st rotating flow that has a subtend face 73a at the entrance side of waste gas 12 brings out plate 73 and brings out plate 74 at a pair of the 2nd rotating flow that the discharge side of waste gas 12 has a subtend face 74a; Bring out linking part that plate 74 links, be in the flat intermediate member 75 that connecting to the 1st rotating flow respectively, to bring out the subtend face 73a of plate 73 different with the subtend face 74a that the 2nd rotating flow brings out plate 74 the 1st rotating flow being brought out plate 73 and the 2nd rotating flow.In the present embodiment, to be configured 90 ° of written treaties different for the 1st rotating flow subtend face 73a that brings out plate 73 and the 2nd rotating flow subtend face 74a that brings out plate 74.
The 1st rotating flow brings out plate 73 and the 2nd rotating flow and brings out plate 74 and form subtriangular shape respectively.And; Because the 1st rotating flow brings out the entrance side that plate 73 is arranged on waste gas 12; The 2nd rotating flow brings out the discharge side that plate 74 is arranged on waste gas 12, so when when the top view rotating flow brings out parts 72, the 1st rotating flow brings out plate 73 and the 2nd rotating flow and brings out plate 74 and compare and be positioned at downside.In addition, intermediate member 75 is dull and stereotyped, brings out the maincenter performance function that plate 74 links as the 1st rotating flow being brought out plate 73 and the 2nd rotating flow.And, the 1st rotating flow is brought out plate 73 be provided with bottom support casting 76, the 2nd rotating flow is brought out plate 74 be provided with upper support plate 77.Through bottom support casting 76, upper support plate 77 rotating flow of adjacency being brought out parts 72 links each other.
Shown in figure 14, bring out parts 72 if waste gas 12 flow into rotating flow, then waste gas 12 and the 1st rotating flow bring out plate 73 subtend face 73a lower face side collision and make gas flow change, the direction of bringing out plate 74 to the 2nd rotating flow flows.Then, waste gas 12 and the 2nd rotating flow bring out the lower face side collision of the subtend face 74a of plate 74, gas flow and then variation.Therefore; Waste gas 12 brings out plate the 73, the 2nd rotating flow through the 1st rotating flow and brings out plate 74 gas flow is changed; Bring out plate the 73, the 2nd rotating flow at the 1st rotating flow and bring out between the plate 74 circuitous flowing, rotate towards the discharge direction of waste gas 12 and flow while bring out the inflow direction of the waste gas 12 of parts 72 from rotating flow.
In addition, in the present embodiment, the subtend face 74a that the subtend face 73a that the 1st rotating flow is brought out plate 73 and the 2nd rotating flow bring out plate 74 be configured to about 90 ° different towards, but the present invention is not limited thereto.The 1st rotating flow bring out the subtend face 73a of plate 73 and subtend face 74a that the 2nd rotating flow brings out plate 74 towards, while so long as can make and flow into the angle that waste gas 12 that rotating flow brings out parts 72 brings out the waste gas 12 of parts 72 from rotating flow inflow direction rotates, flows towards the discharge direction of waste gas 12 and get final product.
In addition; In the present embodiment; Blender 71 is shown in figure 11; Become according to mode and disposed the unit that six rotating flows bring out parts 72, but the present invention is not limited thereto, can the reasonable quantity change that rotating flow brings out parts 72 will be set corresponding to the area of flue 13 etc. with the flow direction quadrature of waste gas 12.
In addition; In the present embodiment; The flow direction at waste gas 12 that blender 71 constitutes one-level has disposed the unit that 6 rotating flows bring out parts 72, but the present invention is not limited thereto, and multistage flow direction at waste gas 12 also can be set dispose the unit that a plurality of rotating flows bring out parts 72.In addition, the direction that the blender 71 of present embodiment can be arranged on the flow direction quadrature of waste gas 12 disposes the unit that a plurality of rotating flows bring out parts 72, and a plurality of flow directions at waste gas 12 are set dispose the unit that a plurality of rotating flows bring out parts 72.
Figure 15 is the figure that schematically illustrates the gas flow of waste gas when in flue, being provided with blender, and Figure 16 is the partial enlarged drawing of Figure 15.Wherein, same with Figure 11 in Figure 15,16, be provided with 6 rotating flows at the width of flue 13 and bring out parts 72.Like Figure 15, shown in 16; Because waste gas 12 brings out plate 73 and the 2nd rotating flow with the 1st rotating flow and brings out plate 74 collisions and make the gas flow variation when bringing out parts 72 through rotating flow; While rotating downside from flue 13 towards last side flow; So bring out between the plate 74 circuitous flowing through bring out plate the 73, the 2nd rotating flow at the 1st rotating flow, can make on one side waste gas 12 rotate, from the downside of flue 13 towards last side flow, so can promote waste gas 12 and HCl gas, NH 3The mixing of gas.
In addition, because blender 71 and the NH that sprays out from spray nozzle 15 4The zone of Cl solution 14 generating gasification is compared and is arranged on back trip side, so can prevent NH 4The drop of Cl solution 14 contact with blender 71 before the generating gasification, so the accumulation of the ash in the burn into waste gas 12 of the breakage of the flue 13 that can prevent to cause because of thermal shock, flue 13 etc.
Figure 17, the 18th, the A-A cutaway view among Fig. 4, Figure 17 schematically illustrate the NH in the waste gas when in flue, blender not being set 3The figure of an example of the CONCENTRATION DISTRIBUTION of gas.Figure 18 schematically illustrates the NH in the waste gas when in flue, being provided with blender 3The figure of an example of the CONCENTRATION DISTRIBUTION of gas.Wherein, in Figure 17, the flue of the existing exhaust treatment system that Reference numeral 104 expressions are shown in Figure 29.
Like Figure 17, shown in 18, the situation of blender 71 is not set compares with the situation that in flue 13, is provided with blender 71, be about to flow into the NH in the waste gas 12 of reduction denitrification apparatus 18 3The deviation of the CONCENTRATION DISTRIBUTION of gas is bigger.
Thereby, because through blender 71 being arranged on the NH that sprays out than from spray nozzle 15 4Back trip side is leaned in the zone of Cl solution 14 generating gasification, can promote NH to the waste gas in the flue 13 12 3So the mixing of gas is NH in the waste gas 12 3The deviation of the CONCENTRATION DISTRIBUTION of gas is suppressed, and can make NH 3The deviation of the CONCENTRATION DISTRIBUTION of gas is for example in the scope about 5%, and is roughly even.Therefore, the reduction efficiency of the NOx that utilizes denitrating catalyst is improved.
In addition, through blender 71 being arranged on the NH that sprays out than from spray nozzle 15 4Back trip side is leaned in the zone of Cl solution 14 generating gasification, except NH 3Outside the gas, can also promote the mixing of HCl gas to the waste gas in the flue 13 12.Therefore, the deviation of the CONCENTRATION DISTRIBUTION of HCl gas is suppressed in the waste gas 12, and the deviation of the CONCENTRATION DISTRIBUTION of HCl gas is also for example in the scope about 5%, and is roughly even.Therefore, the oxidation susceptibility of the Hg that utilizes denitrating catalyst is improved.
In addition, like Figure 11～shown in Figure 14, preferred rotating flow brings out the width L, height D of parts 72 in the scope of following formula (9), (10).
MIN(B、H)/10≤L≤MIN(B、H)…(9)
MIN(B、H)/10≤D≤5×MIN(B、H)…(10)
Wherein, B is the long limit that the flue cross section of position is set, and H is the minor face in flue cross section, and MIN (B, H) is short limit among the minor face H in long limit B, flue cross section in flue cross section.Long limit B, minor face H in the flue cross section are under the situation of equal length, can be any sides.
Rotating flow is brought out the reason that parts 72 are made as in the scope of above-mentioned formula (9), (10) be described below, need to consider NH in the condition, waste gas 12 of the crushing of blender 71 3The viewpoint of the operating condition of the viewpoint of the deviation of concentration, the processability when making, reality, the viewpoint of maintainability etc.
Figure 19 is the figure of the relation between the size of crushing and blender of expression blender.Shown in figure 19, for the crushing that makes blender is below the 25mmAq, need satisfy following formula (11).In addition, in order to make NH in the waste gas 12 3The concentration deviation of concentration is below 5%, need satisfy following formula (12).
MIN(B、H)×D/L 2≥2…(11)
MIN(B、H)×D/L 2≤5…(12)
That is,,, need satisfy above-mentioned formula (11) for the crushing that makes blender 71 is below the 25mmAq as the condition of crushing.In addition, as the effect of blender 71, in order to make NH in the waste gas 12 3The concentration deviation of concentration is below 5%, need satisfy above-mentioned formula (12).
And, the viewpoint of the processability during from manufacturing, the viewpoint of the operating condition of reality, the viewpoint of maintainability, blender 71 need satisfy above-mentioned formula (9), following formula (13).
MIN(B、H)/10≤L≤MIN(B、H)…(9)
MIN(B、H)/10≤D…(13)
According to above-mentioned formula (11), (12), D can be as shown in the formula (14) such expression.
2L 2/MIN(B、H)≤D≤5L 2/MIN(B、H)…(14)
If above-mentioned formula (9) is updated to above-mentioned formula (14), then D can be as shown in the formula (15) such expression.
MIN(B、H)/50≤D≤5×MIN(B、H)…(15)
And if above-mentioned formula (13) is updated to above-mentioned formula (15), then D can represent as above-mentioned formula (10).
MIN(B、H)/10≤D≤5×MIN(B、H)…(10)
Like this, owing to bring out the width L of parts 72, the scope that height D is positioned at above-mentioned formula (9), (10), can a plurality of rotating flows be set in flue 13 and bring out parts 72, so can promote HCl, NH to waste gas 12 through rotating flow 3Mixing.
In addition; The 1st rotating flow brings out the shape that plate 73 and the 2nd rotating flow bring out plate 74; Be not defined as from upper support plate 77 and bottom support casting 76 to intermediate member 75 and the triangle that forms, so long as can make waste gas 12 produce rotating flows, promote waste gas 12 and HCl, NH 3The shape of mixing get final product.For example, the 1st rotating flow brings out the shape that plate 73 and the 2nd rotating flow bring out plate 74, also can be to bring out plate 74 and the 1st rotating flow from the 2nd rotating flow to bring out the distolateral to another distolateral shaped form, waveforms etc. of becoming of plate 73.
Therefore, the emission-control equipment 70 according to present embodiment relates to brings out parts 72 as blender 71 owing to through the profile direction at flue 13 a plurality of rotating flows are set, and can in waste gas 12, promote HCl, NH 3Mixing, so can realize the NH that sprays out by spray nozzle 15 4 Cl solution 14 generating gasification and the NH that produces 3And the homogenising of the CONCENTRATION DISTRIBUTION of HCl.Thus, not only in reduction denitrification apparatus 18, can improve the oxidation susceptibility of Hg and the reducing property of NOx through denitrating catalyst, but also the accumulation of the ash in the burn into waste gas 12 of the breakage of the flue 13 that can prevent to cause because of thermal shock, flue 13 etc.
[embodiment 6]
With reference to accompanying drawing, the emission-control equipment that embodiments of the invention 6 are related to describes.Because the formation of the emission-control equipment 10 that the emission-control equipment that relates to of embodiments of the invention 6 and embodiments of the invention 1 shown in Figure 1 relate to, the emission-control equipment 70 that embodiments of the invention 5 shown in Figure 10 relate to is identical, so only utilize the figure of the formation of representing flue to describe in the present embodiment.The figure that Figure 20 is the emission-control equipment that relates to of embodiments of the invention 6 when the short side direction of flue is observed, Figure 21 are the figure when the long side direction of flue is observed.Wherein, give same Reference numeral to the parts of the formation repetition of the emission-control equipment that relates to embodiment 1 to 5, and omit its explanation.
Like Figure 20, shown in 21, the emission-control equipment that present embodiment relates to is than in flue 13, supplying with NH 4Back trip side and NH are depended in the supply position of Cl solution 14 4The inwall 13a of the flue 13 in the zone of the drop generating gasification of Cl solution 14 is provided with protruding part spare 81.Owing to through the inwall 13a at flue 13 protruding part spare 81 is set, the A/F of the flue 13 that waste gas 12 can circulate diminishes, so can near the wall of flue 13, generate the whirlpool that the air-flow by waste gas 12 forms.HCl gas, NH near the waste gas 12 that therefore, can promote the wall of flue 13, to flow 3The mixing of gas can improve the oxidation susceptibility of Hg, the reducing property of NOx in reduction denitrification apparatus 18.
In addition, for NH 4The drop of Cl solution 14 does not collide with protruding part spare 81, and the position that is provided with of preferred protruding part spare 81 is arranged on the NH that sprays out from spray nozzle 15 4Zone after the drop generating gasification of Cl solution 14, especially preferably be arranged on spray nozzle 15 away from the back trip side position more than the 1m.
In addition, in the emission-control equipment that present embodiment relates to, make being shaped as of protruding part spare 81 tabular, but the present invention is not limited thereto, also can becomes other shapes such as box-shaped, triangle.
[embodiment 7]
With reference to accompanying drawing, the emission-control equipment that embodiments of the invention 7 are related to describes.Because the formation of the emission-control equipment 10 that the emission-control equipment that relates to of embodiments of the invention 7 and embodiments of the invention 1 shown in Figure 1 relate to, the emission-control equipment 70 that embodiments of the invention 5 shown in Figure 10 relate to is identical, so only use the figure of the formation of representing flue to describe in the present embodiment.The figure that Figure 22 is the emission-control equipment that relates to of embodiments of the invention 7 when the short side direction of flue is observed, Figure 23 are the figure when the long side direction of flue is observed.Wherein, give same Reference numeral to the parts of the formation repetition of the emission-control equipment that relates to embodiment 1 to 6, and omit its explanation.
Like Figure 22, shown in 23, the emission-control equipment that present embodiment relates to is than in flue 13, supplying with NH 4The supply position of Cl solution 14 leans on back trip side to be provided with the contraction flow region 82 that the path in the flue 13 is narrowed down.Owing to the contraction flow region 82 that the path in the flue 13 is narrowed down through wall setting at flue 13; Can near the wall of flue 13, generate the whirlpool that the air-flow by waste gas 12 forms, so HCl gas, NH near the waste gas 12 that can promote the wall of flue 13, to flow 3The mixing of gas.Therefore, can suppress HCl gas, NH in the waste gas 12 3The density unevenness of gas can make the oxidation susceptibility of Hg, the reducing property of NOx improve in reduction denitrification apparatus 18.
In addition, in the emission-control equipment that present embodiment relates to, the path of flue 13 narrowed down has formed contraction flow region 82, but the present invention is not limited thereto.For example, also can will be arranged at the wall of flue 13 with contraction flow region 82 identical shaped collapsible part 83 like Figure 24, shown in 25.Thus since can be near collapsible part 83 whirlpool that forms by the air-flow of waste gas 12 of generation, so can promote HCl, the NH near the waste gas 12 mobile wall of flue 13 3Mixing.
In addition, for NH 4The drop of Cl solution 14 does not collide with contraction flow region 82, and the situation that the protruding part spare 81 among position and the embodiment 6 is set of preferred contraction flow region 82 is same, is arranged on the NH that sprays out from spray nozzle 15 4Zone after the drop generating gasification of Cl solution 14 especially preferably is arranged on from spray nozzle 15 away from the back trip side position more than the 1m.
[embodiment 8]
With reference to accompanying drawing, the emission-control equipment that embodiments of the invention 8 are related to describes.Because the formation of the emission-control equipment 10 that the emission-control equipment that relates to of embodiments of the invention 8 and embodiments of the invention 1 shown in Figure 1 relate to, the emission-control equipment 70 that embodiments of the invention 5 shown in Figure 10 relate to is identical, so only utilize the figure of the formation of representing flue to describe in the present embodiment.Figure 26 is the figure of the part of the emission-control equipment that relates to of expression embodiments of the invention 8, and Figure 27 is the local amplification stereogram of the Reference numeral Z among expression Figure 26.Wherein, give same Reference numeral to the parts of the formation repetition of the emission-control equipment that relates to embodiment 1 to 7, and omit its explanation.
Like Figure 26, shown in 27, the emission-control equipment that present embodiment relates on the guide vane 84 of the upstream side that is arranged at reduction denitrification apparatus 18, is provided with promotion HCl gas, NH 3Gas promotes accessory 85 to the mixing that waste gas 12 mixes.Mix to promote that accessory 85 is to a plurality of plate-shaped members that extend with the direction that links a plurality of guide vanes 84 rib 86 quadratures each other.Owing to, can upset the air-flow of waste gas 12, so even if HCl gas, NH in blender 71 in the waste gas 12 through mixing promotion accessory 85 being set to linking guide vane 84 rib 86 each other 3Under the situation of the undercompounding of gas, also can promote HCl gas, NH in the waste gas 12 at the upstream side of reduction denitrification apparatus 18 3The mixing of gas.Therefore, can suppress HCl gas, NH in the waste gas 12 3The density unevenness of gas can make the oxidation susceptibility of the Hg in the reduction denitrification apparatus 18, the reducing property of NOx improve.
[embodiment 9]
With reference to accompanying drawing, the emission-control equipment that embodiments of the invention 9 are related to describes.Figure 28 is the figure of the formation of the emission-control equipment that relates to of schematic representation embodiments of the invention 9.Wherein, because the formation of the emission-control equipment that the emission-control equipment that relates to of present embodiment and embodiment 1 to 8 relate to is identical, thus give same Reference numeral to same parts, and the explanation of omission repetition.
Emission-control equipment 90 shown in figure 28, that present embodiment relates to has the NH of being arranged on 4Between Cl solution feed mechanism 16 and the reduction denitrification apparatus 18 and in flue 13, supply with ammonia (NH 3) gas 91 is as the ammonia (NH of reducing agent 3) gas jet mechanism 92.NH 3There is NH in gas jet mechanism 92 by storage 3The NH of gas 91 3 Gas supply unit 93, with NH 3Ammonia (the NH that gas 91 is carried to flue 13 3) gas carrying path 94 and injection NH in flue 13 3The injection nozzle 95 of gas 91 constitutes.In addition, the NH that sprays from injection nozzle 95 3The emitted dose of gas 91 is adjusted by valve V4.Because NH 3Gas 91 and NH 4The drop of Cl solution 14 that kind is different, even also do not have the infringement that damages flue 13 grades with flue 13 collisions, so also can be to the wall area spray NH of flue 13 3Gas 91.Therefore, can improve NH in the low concentration region of wall edge of flue 13 3Concentration can suppress HCl gas, NH in the waste gas 12 3The density unevenness of gas.
In addition, be from NH preferably from the position that injection nozzle 95 is supplied with in flue 13 4The spray position of Cl solution 14 is left the above back trip side of 1m.This is in order to prevent NH 4The drop of Cl solution 14 and injection nozzle 95 collisions.
Therefore, the emission-control equipment 90 that relates to according to present embodiment since through to flue 13 internal sprayings NH 4After the Cl solution 14, utilize NH 3NH sprays in gas jet mechanism 92 in flue 13 3Gas 91 can improve the NH in the low concentration region of wall edge of flue 13 3Concentration is so not only can tackle HCl gas, NH in the waste gas 12 3The density unevenness of gas, but also can keep the oxidation susceptibility of Hg in the denitrification apparatus 18 in reduction, improve the reducing property of NOx simultaneously.
<nH 3The Kong Zhi > of the emitted dose of gas;
Upstream side at spray nozzle 15 is provided with the flowmeter 51 that the flow of waste gas 12 is carried out instrumentation, determines the flow of waste gas 12 thus.Based on the flow value of the waste gas that is determined by flowmeter 51 12, control device 52 can be adjusted the NH that sprays from injection nozzle 95 3The flow of gas 91, angle, initial velocity etc.
Thereby, NOx concentration and the balance of Hg concentration and different usually the waste gas 12 of discharging from boiler 11 combustion apparatus such as grade, NOx concentration is higher, can only be to flue 13 internal spraying NH 4Cl solution 14 and can't supply with the NH of necessary amount 3The time, through in flue 13, spraying NH from injection nozzle 95 3Gas 91 can reduce the HCl gas, the NH that are supplied in the waste gas 12 in the flue 13 3The deviation of the CONCENTRATION DISTRIBUTION of gas is supplied with to waste gas 12 simultaneously NOx is reduced the NH of necessary amount 3Gas.Therefore, can tackle HCl gas, NH in the waste gas 12 3The density unevenness of gas, and, can in reduction denitrification apparatus 18, improve the oxidation susceptibility of Hg, the reducing property of NOx.
In addition, by NH 3The NH that gas supply unit 93 is supplied with 3The quantity delivered of gas 91 can utilize the value of NOx densimeter 53 to control.
In addition, in the emission-control equipment 90 that present embodiment relates to, NH can only be set 3 Gas supply unit 93 in flue 13, supplies with NH 3Gas 91, but the present invention is not limited thereto.Also can replace NH 3 Gas supply unit 93 and be provided with in flue 13 and supply with hydrogen chloride (HCl) gas supply part of hydrogen chloride (HCl) gas, supply HCl gas to flue 13 in as oxidizing gas.Thus, can in waste gas 12, supply with HCl gas with the necessary amount of Hg oxidation.In addition, can adjust spray amount, spray angle, the initial velocity of the HCl gas of supplying with by above-mentioned HCl gas supply part based on the flow velocity of the waste gas that determines by flowmeter 51 12.
And, NH can also be set 3 Gas supply unit 93 and above-mentioned HCl gas supply part both sides.Can be based on the flow velocity of the waste gas that determines by flowmeter 51 12, adjustment is by NH 3The NH that gas supply unit 93 and above-mentioned HCl gas supply part are supplied with 3The spray amount of gas 91 and HCl gas, spray angle, initial velocity.Thus, owing to waste gas 12 is carried out NH through other approach 3The supply of gas and HCl gas is so even under the situation of NOx in waste gas 12 or Hg concentration change that kind, also can carry out suitable reply.
As the employed oxidation promoter of oxidizing gas, be not limited to HCl, also can use hydrogen bromide (HBr) beyond the HCl, hydrogen iodide hydrogen halides such as (HI) as oxidizing gas.
[utilizability in the industry]
As stated, the emission-control equipment that the present invention relates to is owing to can supply with the NH to the flue internal spraying according to the mode of the inwall that is not attached to flue 4Cl solution promotes by NH 4HCl gas, NH that the drop of Cl solution produces 3Gas mixes with waste gas, so be applicable to the emission-control equipment that the Hg in the waste gas, NOx are removed.
10,70, the 90-emission-control equipment description of reference numerals:; The 11-boiler; 12-waste gas; The 13-flue; 14-ammonium chloride (NH 4Cl) solution; 15,61-spray nozzle; 16-ammonium chloride (NH 4Cl) solution feed mechanism (reduction-oxidation auxiliary agent feed mechanism); 18-reduction denitrification apparatus (reduction denitration mechanism); 19-heat exchanger (air heater); The 20-dust arrester; 21-lime stone-gypsum slurry; The 22-wet desulfurizer; 25-ammonium chloride (NH 4Cl) solution supply pipe; 26,33,47-air; 27,34-air supply pipe; 28-ammonium chloride (NH 4Cl) NaOH solution tank NaOH; 31,36-air supply unit; 32-is blown into pipe; The 35-spray-hole; The 37-slit; 38-1～38-3-denitrating catalyst layer; The 39-cowling panel; The 41-apparatus main body; 42-absorption liquid pipeline; The 43-nozzle; The 44-Purge gas; The 45-chimney; 46-water; The 48-dehydrator; The 49-gypsum; The 51-flowmeter; The 52-control device; The 53-NOx densimeter; 54-1,54-2-mercury (Hg) densimeter; The 55-tower bottom; 56-oxidation reduction potential determination control device (ORP controller); 71-blender (mixed organization); The 72-rotating flow brings out parts; 73-the 1st rotating flow brings out plate; 74-the 2nd rotating flow brings out plate; 75-intermediate member (linking part); The 76-bottom support casting; The 77-upper support plate; 81-protruding part spare; The 82-contraction flow region; The 83-collapsible part; The 84-guide vane; 85-mixes the promotion accessory; The 86-rib; 91-ammonia (NH 3) gas; 92-ammonia (NH 3) gas jet mechanism; 93-NH 3The gas supply unit; 94-ammonia (NH 3) the gas carrying path; The 95-injection nozzle; V1～V4-valve.

Claims (17)

1. emission-control equipment, will waste gas from boiler in contained nitrogen oxide, mercury remove, it is characterized in that having:
Reduction-oxidation auxiliary agent feed mechanism is in the flue of the reduction-oxidation auxiliary agent that generates oxidizing gas and reducibility gas when it utilizes a plurality of spray nozzles to gasify with the liquid downstream that are sprayed to said boiler;
Reduction denitration mechanism, its have with said reducibility gas reduce said nitrogen oxides from exhaust gas and under said oxidizing gas coexistence with the denitrating catalyst of mercury oxidation; With
Wet type desulfurizing mechanism, the mercury after it utilizes the alkali absorption liquid will be in this reduces denitration mechanism oxidized is removed;
Said spray nozzle is not attached to the mode of the inwall of said flue according to said reduction-oxidation auxiliary agent, and this reduction-oxidation auxiliary agent is supplied with in said flue.
2. emission-control equipment according to claim 1 is characterized in that,
Droplets vaporize based on obtaining according to gas flow rate, drop initial velocity, liquid-drop diameter, EGT, drop temperature at least is needed apart from l and spray angle α; Satisfy the mode of following formula according to the beeline x of the inwall of the nozzle bore of said spray nozzle and said flue; Dispose said spray nozzle
x＞l×sinα…(1)。
3. according to claim 1 or 2 described emission-control equipments, it is characterized in that,
Said reduction-oxidation auxiliary agent is an ammonium chloride.
4. according to any described emission-control equipment in the claim 1 to 3, it is characterized in that,
The nozzle bore of said spray nozzle is set at the above position of wall 0.5m of the said flue of distance.
5. according to any described emission-control equipment in the claim 1 to 4, it is characterized in that,
The nozzle bore of a plurality of spray nozzles is configured to satisfy following formula:
a≤b/5…(2)，
Wherein, a is that the injector spacing of spray nozzle leaves, and b is the length of long side in the cross-sectional length of flue.
6. according to any described emission-control equipment in the claim 1 to 5, it is characterized in that,
Said spray nozzle has the nozzle bore of the said reduction-oxidation auxiliary agent of a plurality of sprayings.
7. emission-control equipment according to claim 6 is characterized in that,
Said nozzle bore being spaced apart below the 0.3m each other.
8. according to any described emission-control equipment in the claim 1 to 7, it is characterized in that,
Spray amount from each said spray nozzle can change.
9. according to any described emission-control equipment in the claim 1 to 8, it is characterized in that,
Have perhaps both sides of any side of being arranged in the hydrogen chloride gas supply unit of supplying with the ammonia supply unit of ammonia between said reduction-oxidation auxiliary agent feed mechanism and the said reduction denitration mechanism and in said flue and in said flue, supplying with hydrogen chloride gas.
10. the mercury of a waste gas is removed method, will waste gas from boiler in contained nitrogen oxide, mercury remove, it is characterized in that having:
Reduction-oxidation auxiliary agent supplying step, the reduction-oxidation auxiliary agent that generates oxidizing gas and reducibility gas when utilizing a plurality of spray nozzles to gasify is with in the liquid flue that is sprayed to said boiler;
Reduction denitration treatment step use denitrating catalyst, utilizes said reducibility gas that said nitrogen oxides from exhaust gas is reduced, and under said oxidizing gas coexists with mercury oxidation; With
The wet type desulfurizing step, the mercury after utilizing the alkali absorption liquid will be in this reduces the denitration treatment step oxidized is removed;
Said spray nozzle is not attached to the mode of the inwall of said flue according to said reduction-oxidation auxiliary agent, and this reduction-oxidation auxiliary agent is supplied with in said flue.
11. the mercury of waste gas according to claim 10 is removed method, it is characterized in that,
Droplets vaporize based on obtaining according to gas flow rate, drop initial velocity, liquid-drop diameter, EGT, drop temperature at least is needed apart from l and spray angle α; Satisfy the mode of following formula according to the beeline x of the inwall of the nozzle bore of said spray nozzle and said flue; Dispose the nozzle bore of said spray nozzle
x＞l×sinα…(3)。
12. the mercury according to claim 10 or 11 described waste gas is removed method, it is characterized in that,
Said reduction-oxidation auxiliary agent is an ammonium chloride.
13. the mercury according to any described waste gas in the claim 10 to 12 is removed method, it is characterized in that,
The nozzle bore of said spray nozzle is arranged on the position more than the distance wall 0.5m of said flue.
14. the mercury according to any described waste gas in the claim 10 to 13 is removed method, it is characterized in that,
The nozzle bore of a plurality of spray nozzles is configured to satisfy following formula:
a≤b/5…(4)，
Wherein, a is that the injector spacing of spray nozzle leaves, and b is the length of long side in the cross-sectional length of flue.
15. the mercury according to any described waste gas in the claim 10 to 14 is removed method, it is characterized in that,
Have in the flow measurement step of measuring the flow velocity of said waste gas than the supply position of supplying with said reduction-oxidation auxiliary agent by upstream side,
Adjust spray amount, spray angle, the initial velocity of said reduction-oxidation auxiliary agent based on the flow velocity of the said waste gas that determines.
16. the mercury according to any described waste gas in the claim 10 to 15 is removed method, it is characterized in that, comprising:
In the preceding step side of said reduction denitration treatment step, the nitrous oxides concentration determination step that the concentration of said nitrogen oxides from exhaust gas is measured; With
In the back step side of said reduction denitration treatment step, the mercury concentration determination step that the concentration of the mercury in the said waste gas is measured;
Based on the concentration of the said nitrogen oxides from exhaust gas that obtains by said nitrous oxides concentration determination step with by any side or both sides in the concentration of the mercury in the said waste gas of said mercury concentration determination step acquisition, be adjusted at the quantity delivered of the said reduction-oxidation auxiliary agent of supplying with in the said reduction-oxidation auxiliary agent supplying step.
17. the mercury according to claim 15 or 16 described waste gas is removed method, it is characterized in that,
Between said reduction-oxidation auxiliary agent supplying step and said reduction denitration treatment step; Comprise any side or both sides in the hydrogen chloride gas supplying step of in said flue, supplying with the ammonia supplying step of ammonia and in said flue, supplying with hydrogen chloride gas
Based on the flow velocity of the said waste gas that is gone out by said flow measurement step measurements, any side in the said hydrogen chloride gas of supplying with to the said ammonia supplied with by said ammonia supplying step, by said hydrogen chloride gas supplying step perhaps adjust by both sides' spray amount, spray angle, initial velocity.
CN201080034421.6A 2009-08-05 2010-08-05 The mercury removing method of emission-control equipment and waste gas Active CN102470318B (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
JP2009182710A JP5558042B2 (en) 2009-08-05 2009-08-05 Exhaust gas treatment device and mercury removal method of exhaust gas
JP2009-182710 2009-08-05
PCT/JP2010/063673 WO2011016585A1 (en) 2009-08-05 2010-08-05 Device for treating exhaust gas and method for eliminating mercury from exhaust gas

Publications (2)

Publication Number Publication Date
CN102470318A true CN102470318A (en) 2012-05-23
CN102470318B CN102470318B (en) 2015-09-23

Family

ID=43544477

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201080034421.6A Active CN102470318B (en) 2009-08-05 2010-08-05 The mercury removing method of emission-control equipment and waste gas

Country Status (6)

Country Link
US (1) US9084965B2 (en)
EP (1) EP2463016A4 (en)
JP (1) JP5558042B2 (en)
CN (1) CN102470318B (en)
CA (1) CA2769861C (en)
WO (1) WO2011016585A1 (en)

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103727553A (en) * 2013-12-18 2014-04-16 西安西热锅炉环保工程有限公司 Enhanced system and method for adsorption removal of mercury in coal-fired flue gas
CN103768943A (en) * 2014-01-23 2014-05-07 天津大学 Smoke desulfurization and denitrification method and device of fuel engine
CN104619399A (en) * 2012-09-14 2015-05-13 三菱日立电力系统株式会社 System for treating mercury in exhaust gas
CN108479389A (en) * 2018-04-27 2018-09-04 华中科技大学 A kind of flue gas collaboration denitration demercuration system and method
CN108854523A (en) * 2018-07-03 2018-11-23 上海帅腾环保科技有限公司 A kind of construction of environmental protection removes nitre device with factory's flue gas desulfurization
CN109603456A (en) * 2019-01-25 2019-04-12 米凯利科技（北京）有限公司 Utilize the dry method flue gas demercuration system of halide crystal
CN113660998A (en) * 2019-04-10 2021-11-16 P&F机械股份有限公司 Apparatus and method for producing enameled wire

Families Citing this family (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8449851B2 (en) * 2009-11-16 2013-05-28 Ihi Corporation Mercury removing system and mercury removing method
JP5529701B2 (en) * 2010-09-28 2014-06-25 三菱重工業株式会社 Gas analyzer, mercury removal system, and mercury removal method
US9217353B2 (en) 2013-04-03 2015-12-22 Caterpillar Inc. Mixer for fluid injection system
US9664082B2 (en) 2014-06-02 2017-05-30 Caterpillar Inc. Reductant dosing system having staggered injectors
CN104028101B (en) * 2014-06-23 2016-04-13 李玢 Flue gas desulfurizing and hydrargyrum-removing integral system and technique
JP6535555B2 (en) 2015-09-14 2019-06-26 三菱日立パワーシステムズ株式会社 boiler
CN106943861A (en) * 2017-04-18 2017-07-14 北京清新环境技术股份有限公司 A kind of removing sulfur trioxide devices and methods therefor suitable for large scale section flue
CN107754578A (en) * 2017-10-20 2018-03-06 佛山市莫森环境工程有限公司 A kind of industry coal-boiler flue gas minimum discharge complete set of equipments
JP7254465B2 (en) * 2018-08-29 2023-04-10 Ｕｂｅ三菱セメント株式会社 Mercury recovery device and mercury recovery method
CN109847547A (en) * 2019-04-08 2019-06-07 重庆中科检测技术服务有限公司 A kind of heavy metal chelant and preparation method thereof
CN113181757A (en) * 2021-03-11 2021-07-30 北京鑫晟环能科技发展有限公司 Chlorosilane waste gas atomization treatment device
CN114749044A (en) * 2022-05-07 2022-07-15 中钢集团天澄环保科技股份有限公司 Fast mixing device for spraying powder in splashing type flue

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5314664A (en) * 1976-07-27 1978-02-09 Nippon Steel Corp Method for removing nitrogen oxides contained
EP0860197A1 (en) * 1997-02-19 1998-08-26 Mitsubishi Heavy Industries, Ltd. Process for treating exhaust gas and exhaust gas treating equipment
US20050147549A1 (en) * 2004-01-06 2005-07-07 General Electric Company Method and system for removal of NOx and mercury emissions from coal combustion
JP2009154067A (en) * 2007-12-26 2009-07-16 Mitsubishi Heavy Ind Ltd Apparatus and method for treatment of exhaust gas

Family Cites Families (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5342592A (en) 1989-07-04 1994-08-30 Fuel Tech Europe Ltd. Lance-type injection apparatus for introducing chemical agents into flue gases
US5118481A (en) * 1990-11-09 1992-06-02 Energy And Environmental Research Corporation Methods for reducing NOx emissions from combustion effluents
US5489419A (en) 1992-10-13 1996-02-06 Nalco Fuel Tech Process for pollution control
ES2140665T3 (en) 1994-03-21 2000-03-01 Seghers Better Technology Grou PROCEDURE AND DEVICE FOR INTRODUCING A LIQUID OR GASEOUS TREATMENT FLUID IN A SMOKE GAS FLOW.
US6030204A (en) * 1998-03-09 2000-02-29 Duquesne Light Company Method for NOx reduction by upper furnace injection of solutions of fixed nitrogen in water
JP2001198434A (en) * 2000-01-18 2001-07-24 Mitsubishi Heavy Ind Ltd Method for treating mercury in exhaust gas and treatment system of exhaust gas
US6610263B2 (en) * 2000-08-01 2003-08-26 Enviroscrub Technologies Corporation System and process for removal of pollutants from a gas stream
US6960329B2 (en) 2002-03-12 2005-11-01 Foster Wheeler Energy Corporation Method and apparatus for removing mercury species from hot flue gas
US7118721B2 (en) * 2002-11-26 2006-10-10 Alstom Technology Ltd Method for treating emissions
KR100597961B1 (en) * 2003-04-24 2006-07-06 한국남부발전 주식회사 Cleaning Method of NO2 Visible Gas from Stationary Sources
JP2004332611A (en) * 2003-05-07 2004-11-25 Nec Kansai Ltd Mechanism for preventing clogging of exhaust pipe
CA2556649C (en) * 2004-02-26 2012-07-10 Pursuit Dynamics Plc Improvements in or relating to a method and apparatus for generating a mist
JP4838579B2 (en) 2005-12-21 2011-12-14 三菱重工業株式会社 Mercury removal system and mercury removal method
JP4719171B2 (en) 2007-03-09 2011-07-06 三菱重工業株式会社 Exhaust gas treatment apparatus and method
US7906090B2 (en) * 2009-07-06 2011-03-15 Mitsubishi Heavy Industries, Ltd. Mercury reduction system and mercury reduction method of flue gas containing mercury

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5314664A (en) * 1976-07-27 1978-02-09 Nippon Steel Corp Method for removing nitrogen oxides contained
EP0860197A1 (en) * 1997-02-19 1998-08-26 Mitsubishi Heavy Industries, Ltd. Process for treating exhaust gas and exhaust gas treating equipment
US20050147549A1 (en) * 2004-01-06 2005-07-07 General Electric Company Method and system for removal of NOx and mercury emissions from coal combustion
JP2009154067A (en) * 2007-12-26 2009-07-16 Mitsubishi Heavy Ind Ltd Apparatus and method for treatment of exhaust gas

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104619399A (en) * 2012-09-14 2015-05-13 三菱日立电力系统株式会社 System for treating mercury in exhaust gas
CN104619399B (en) * 2012-09-14 2016-08-31 三菱日立电力系统株式会社 Hydrargyrum processing system in aerofluxus
CN103727553A (en) * 2013-12-18 2014-04-16 西安西热锅炉环保工程有限公司 Enhanced system and method for adsorption removal of mercury in coal-fired flue gas
CN103768943A (en) * 2014-01-23 2014-05-07 天津大学 Smoke desulfurization and denitrification method and device of fuel engine
CN108479389A (en) * 2018-04-27 2018-09-04 华中科技大学 A kind of flue gas collaboration denitration demercuration system and method
CN108479389B (en) * 2018-04-27 2021-03-26 华中科技大学 Flue gas synergistic denitration and demercuration system and method
CN108854523A (en) * 2018-07-03 2018-11-23 上海帅腾环保科技有限公司 A kind of construction of environmental protection removes nitre device with factory's flue gas desulfurization
CN109603456A (en) * 2019-01-25 2019-04-12 米凯利科技（北京）有限公司 Utilize the dry method flue gas demercuration system of halide crystal
CN109603456B (en) * 2019-01-25 2021-08-03 米凯利科技（北京）有限公司 Dry flue gas demercuration system using halide crystals
CN113660998A (en) * 2019-04-10 2021-11-16 P&F机械股份有限公司 Apparatus and method for producing enameled wire

Also Published As

Publication number Publication date
WO2011016585A1 (en) 2011-02-10
JP5558042B2 (en) 2014-07-23
EP2463016A1 (en) 2012-06-13
US9084965B2 (en) 2015-07-21
US20120189521A1 (en) 2012-07-26
JP2011031222A (en) 2011-02-17
CA2769861C (en) 2014-06-03
CA2769861A1 (en) 2011-02-10
EP2463016A4 (en) 2012-12-26
CN102470318B (en) 2015-09-23

Similar Documents

Publication Publication Date Title
CN102470318B (en) The mercury removing method of emission-control equipment and waste gas
CN102470319B (en) Emission-control equipment
US7906090B2 (en) Mercury reduction system and mercury reduction method of flue gas containing mercury
CN110075702B (en) Device for simultaneously removing nitrogen oxides (NOx) and sulfur oxides (SOx) in exhaust gas
JP5693061B2 (en) Exhaust gas treatment equipment
EP2444143B1 (en) System for removing mercury and method of removing mercury from mercury-containing high-temperature discharge gas
EP2444144B1 (en) System for removing mercury and method of removing mercury from mercury-containing high-temperature discharge gas
US7901645B2 (en) Mercury reduction system and mercury reduction method of flue gas containing mercury
EP2772301B1 (en) Process and apparatus for reducing the content of nitrogen oxides
CN114849471A (en) HTr-3SO combined denitration system applied to treatment of glass fiber kiln waste gas
WO2010146672A1 (en) System for removing mercury and method of removing mercury from mercury-containing high-temperature discharge gas
US8071036B2 (en) Mercury reduction system
JP2018130672A (en) Exhaust gas treatment method and exhaust gas treatment apparatus
JP2014149148A (en) Mercury removal system and mercury removal method from high-temperature exhaust gas containing mercury

Legal Events

Date Code Title Description
C06 Publication
PB01 Publication
C10 Entry into substantive examination
SE01 Entry into force of request for substantive examination
ASS Succession or assignment of patent right

Owner name: MITSUBISHI HITACHI POWER SYSTEM LTD.

Free format text: FORMER OWNER: MITSUBISHI JUKOGIO KK

Effective date: 20150304

C41 Transfer of patent application or patent right or utility model
TA01 Transfer of patent application right

Effective date of registration: 20150304

Address after: Kanagawa

Applicant after: Mitsubishi Hitachi Power System Ltd.

Address before: Tokyo, Japan

Applicant before: Mit-subishi Heavy Industries Ltd.

C14 Grant of patent or utility model
GR01 Patent grant
CP01 Change in the name or title of a patent holder
CP01 Change in the name or title of a patent holder

Address after: Kanagawa Prefecture, Japan

Patentee after: Mitsubishi Power Co., Ltd

Address before: Kanagawa Prefecture, Japan

Patentee before: MITSUBISHI HITACHI POWER SYSTEMS, Ltd.